Cpox reactor control system and method

ABSTRACT

A fuel reformer module ( 8005 ) for initiating catalytic partial oxidation (CPOX) to reform a hydrocarbon fuel oxidant mixture ( 2025, 3025 ) to output a syngas reformate ( 2027 ) to solid oxide fuel cell stack ( 2080, 5040 ). A solid non-porous ceramic catalyzing body ( 3030 ) includes a plurality of catalyst coated fuel passages ( 3085 ). A thermally conductive element ( 9005, 10005, 11005, 13005 ), with a coefficient of thermal conductivity of 50 W/m° K or greater is thermally conductively coupled with the catalyzing body. A first thermal sensor ( 8030 ) is thermally conductively coupled with the thermally conductive element. A second thermal sensor is thermally conductively coupled with a surface of the fuel cell stack. A control method independently modulates an oxidant input flow rate, based on first thermal sensor signal values, a hydrocarbon fuel input flow rate, based on second thermal sensor signal values.

1 CROSS REFERENCE TO RELATED U.S. PATENT APPLICATIONS

The present application claims the benefit of U.S. Provisional PatentApplication Ser. No. 62/243,960 entitled Improved CPOX Fuel Reformer andSOFC System, filed Oct. 20, 2015 under 55 U.S.C. § 119(e) and is acontinuation-in-part of non-provisional U.S. patent application Ser. No.15/287,402 entitled SOFC System Formed with Multiple ThermallyConductive Pathways, filed on Oct. 6, 2016, each of which isincorporated herein by reference in its entirety and for all purposes.

2 COPYRIGHT NOTICE

A portion of the disclosure of this patent document may contain materialthat is subject to copyright protection. The copyright owner has noobjection to the facsimile reproduction by anyone of the patent documentor the patent disclosure, as it appears in the Patent and TrademarkOffice patent files or records, but otherwise reserves all copyrightrights whatsoever. The following notice shall apply to this document:Copyright © Protonex Technology Corporation 2015.

3 BACKGROUND

3.1 Field

The exemplary, illustrative technology described herein relates to SolidOxide Fuel Cell (SOFC) systems and particularly to structural featuresand methods of making enclosure walls from thermally conductivematerials and forming the enclosures to provide thermally conductivepathways designed to distribute thermal energy by thermal conduction ina desired manner. More specifically the technology relates to thermalenergy management in an SOFC system by providing thermally conductivepathways configured to improve operating performance, safety, andreliability.

3.2 The Related Art

Conventional solid oxide fuel cell (SOFC) systems used to generateelectrical energy by an electrochemical process that typically utilizedgas to gas heat exchangers to transfer thermal energy from exhaust gasesto incoming air. Example embodiments are disclosed in U.S. Pat. No.8,557,451 entitled Fuel Processor for Fuel Cell System, issued Oct. 15,2013 and in U.S. Pat. No. 8,197,976 entitled Solid Oxide Fuel CellSystem with Hot Zones and Two-Stage Tail Gas Combustors. While thegas-to-gas heat exchangers transfer waste heat from exhaust gases toincoming cathode air, the overall systems operate with hot spots at thetail gas combustion chamber and other locations where fuel is beingcombusted.

In conventional SOFC systems, the temperature surrounding hot spotstends to exceed a safe operating temperature for many highly thermallyconductive metals such as copper and aluminum. Additionally, highlythermally conductive metals such as copper and aluminum are oftendamaged by oxidation when exposed to oxygen rich cathode gasses used inconventional SOFC systems. This has led to reluctance in the art to usehighly thermally conductive metals with conventional SOFC systems whichare instead constructed with temperature resistant metals surroundingthe hot spots to avoid burn through and other failures includingshortened product life caused by metal oxidation. The temperatureresistant metals tend to include elevated temperature resident superalloys usually comprising nickel and cobalt such as Hastelloy, Monel,Inconel, and others that are less likely to be damaged by prolongedelevated temperature and oxygen exposure. One problem with usingelevated temperature resistant super alloys is that they have a lowcoefficient of thermal conductivity such as less than about 40 W/m° Kand more generally less than 20 W/m° K. As compared with more thermallyconductive metals (e.g. aluminum and copper alloys) with a coefficientof thermal conductivity of more than 200 W/m° K, the elevatedtemperature resistant super alloys are poorer thermal conductors. As aresult, heat transfer by thermal conduction in conventional SOFCenclosures is slow and the slow rate of thermal conduction tends tocreate permanent hot spots or temperature gradients in the overallstructure of the SOFC system.

More recently SOFC systems have been constructed to promote thermalenergy transfer by thermal conduction to reduce thermal gradients. Onesuch system is disclosed in U.S. application Ser. No. 14/399,795entitled SOFC-Conduction published Apr. 7, 2016 as US: 20160099476A1.This document discloses an SOFC system that is formed with inner andouter metal enclosures formed as thermally conductive pathways made frommore thermally conductive metals such as aluminum and copper alloys inorder to improve the rate of thermal conduction from hot spots to coolerareas of the structure. By providing a thermally conductive pathway witha higher coefficient of thermal conductivity and providing some wallswith a larger thermal mass than others, thermal gradients are reduced aseach different enclosure wall system tends to more rapidly normalize toa uniform temperature enabled by more rapid thermal conduction throughthe aluminum and copper enclosure walls which in some cases include acopper core.

Conventional SOFC systems utilize internal temperature sensors tomeasure instantaneous temperature at hot spot locations located insidehot zones of the SOFC system. An electric controller monitors theinstantaneous temperature reported by each internal temperature sensor.If an over temperature condition is detected, the electronic controlleris operable to shut down operation of the SOFC system by closing aninput fuel valve. However, one problem with the use of internal sensorsin an elevated temperature environment is that the thermal sensors canfail to provide the instantaneous internal temperature at all or canprovide an inaccurate instantaneous temperature. As a result of adamaged or inaccurate internal thermal sensor an over temperaturecondition goes undetected and that can cause catastrophic failure suchas a burn through of one of the enclosure walls. Other consequencesinclude damage to thermal insulation surrounding hot zones and or damageto coating layers applied to internal and external enclosure wallsurfaces. Even when damage due to an over temperature condition isminimal, when internal temperature sensors fail they need to bereplaced. To replace a damaged internal temperature sensor the SOFCsystem must be disassembled and this is costly.

In view of the foregoing discussion there is a need in the art toprovide an SOFC system that uses external temperature sensors to detectover temperature operating conductions that may lead to system damage orfailure without relying on internal sensors. There is a further need inthe art to provide a passive backup to thermal sensors that detect overtemperature conditions. The passive back is provided to shut down theSOFC system if the temperature sensor fails or otherwise reports aninaccurate temperature.

4 SUMMARY

The present disclosure solves problems relating to controlling a solidoxide fuel cell system and controlling a catalytic partial oxidation(CPOX) fuel reformer operating to reform a mixture of hydrocarbon fueland an oxidant, e.g. air. The syngas reformate is delivered to the anodeside of a plurality of solid oxide fuel cells (SOFC) operating togenerate electrical power. The CPOX reformer of the present disclosureincludes a control system and a control method for monitoring changes ina temperature of each the CPOX reaction and changes in a temperature orthe SOFC reaction as well as control elements for independentlymodifying an input flow rate of the hydrocarbon fuel and independentlymodifying an input flow rate of the oxidant.

A fuel reformer module of the present disclosure initiates a CPOXreaction to reform a hydrocarbon fuel oxidant mixture into a syngasreformate. The fuel reformer module includes catalyzing body, having aninput end for receiving the hydrocarbon fuel oxidant mixture therein andan output end for delivering the syngas reformate therefrom. Thecatalyzing body is formed from a solid non-porous ceramic substrate witha plurality of independent catalyst fuel passages extending between theinput end and an output end of each fuel passage. An inside surface ofeach catalyst fuel passages is coated with a catalyst layer comprising amaterial selected to initiate the CPOX reaction. A thermally conductiveelement, comprising a material having a coefficient of thermalconductivity of 50 W/m° K or greater and preferably 100 W/m° K orgreater is thermally conductively coupled with the catalyzing body overa contact surface area. The contact surface area can be an external orinternal surface of the catalyzing body and preferably extends along alongitudinal axis of the catalyzing body. A first thermal sensor isthermally conductively coupled with the thermally conductive element.The first thermal sensor generates a first temperature signalcorresponding with a surface temperature of the thermally conductiveelement proximate to whatever surface of the thermally conductiveelement the first thermal sensor is coupled to.

An SOFC system of the present disclosure includes the above describedfuel reformer module and a fuel oxidant control module configured to mixthe hydrocarbon fuel oxidant mixture in various proportion. The fueloxidant control module is disposed between a hydrocarbon fuel supplysource and an oxidant supply source and the input end of the catalyzingbody. A hydrocarbon fuel flow rate modulator is disposed between thehydrocarbon fuel source and the input end. An oxidant flow ratemodulator is disposed between the oxidant source and the input end. Anelectronic controller is operated to transmit independent command andcontrol signals to each of the hydrocarbon fuel flow rate modulator andthe oxidant flow rate modulator.

The SOFC system includes a solid oxide fuel cell (SOFC) stack comprisinga plurality individual SOFC fuel cells each comprising a solid oxideanode electrode layer. The syngas reformate output from the fuelreformer module is directed to flow over the solid oxide anode electrodelayers to initiate and maintain an SOFC reaction. A hot zone enclosurecomprises a plurality of hot zone enclosure walls that are joinedtogether to enclose a hot zone cavity surrounding the SOFC stack. Thehot zone enclosure walls are formed from materials having a coefficientof thermal conductivity of 100 W/m° K or greater and are joined togetherusing to form a first continuous thermally conductive pathway thatincludes all the hot zone enclosure walls. A second thermal sensor isthermally conductively coupled with a surface of the first thermallyconductive pathway for generating a second temperature signalcorresponding with a temperature of the surface of the first thermallyconductive pathway that he second thermal sensor is coupled to.

A range of first set point temperature values are stored by theelectronic controller. The range of first set point values correspondswith a calibrated operating temperature range know to produce the syngasreformate having a desired syngas composition. In one example the firstset point temperature values correspond with a syngas composition has alow percentage of unreacted hydrocarbon fuel molecules. A range ofsecond set point temperature values are stored by the electroniccontroller. The range of second set point values corresponds with acalibrated operating temperature range know to produce a desiredperformance characteristic of the SOFC stack. In one example the secondset point temperature values correspond with a fuel to electrical powerefficiency rating.

The electronic controller operates a first control loop based onsampling the first thermal sensor signal values. The first control loopcommands the oxidant flow rate modulator to increase or decrease theoxidant flow rate to maintain the sampled first temperature signalvalues within the range of first set point values. The electroniccontroller operates a second control loop based on sampling secondthermal sensor signal values. The second control loop commands thehydrocarbon fuel flow rate modulator to increase or decrease thehydrocarbon fuel flow rate to maintain the sampled second temperaturesignal values within the range of second set point values.

A method for controlling the SOFC system included delivering ahydrocarbon fuel and oxidant mixture into the input end of thecatalyzing body. A hydrocarbon fuel flow rate modulator is disposedbetween a hydrocarbon fuel supply source and the input end of thecatalyst body. An oxidant flow rate modulator disposed between anoxidant supply source and the input end of the catalyst body. Theelectronic controller delivers first command and control signals to theoxidant flow rate modulator to modulate an oxidant flow rate. Theelectronic controller delivers second command and control signals to thehydrocarbon fuel flow rate modulator to modulate a hydrocarbon fuel flowrate. An input manifold provided between the catalyst body output endand an SOFC stack delivers the syngas reformate output from the catalystbody to the solid oxide anode electrodes of the solid oxide fuel cell(SOFC) stack to initiate an SOFC reaction at an SOFC reactiontemperature. The electronic controller samples the first temperaturecontrol signals generated by the first temperature sensor and alsosampled second temperature control signals generated by a secondtemperature sensor. The electronic controller stores a range of firstset point temperature values corresponding with a desired composition ofthe syngas reformate being output from the fuel reformer module andstores a range of second set point temperature values corresponding witha desired performance characteristic of the SOFC stack. The electroniccontroller operates a first control loop based on sampling firsttemperature sensor signal values and commanding the oxidant flow ratemodulator to increase or decrease the oxidant flow rate to maintain thesampled first temperature signal values within the range of first setpoint values. The electronic controller operates a second control loopbased on sampling second thermal sensor signal values and commanding thehydrocarbon fuel flow rate modulator to increase or decrease thehydrocarbon fuel flow rate to maintain the sampled second temperaturesignal values within the range of second set point values.

5 BRIEF DESCRIPTION OF THE DRAWINGS

The features of the present disclosure will best be understood from adetailed description of the subject technology and example embodimentsthereof selected for the purposes of illustration and shown in theaccompanying drawings in which:

FIG. 1 depicts a schematic view of a non-limiting exemplary SOFC systemembodiment according to the present disclosure.

FIG. 2 depicts a schematic side section view taken through anon-limiting exemplary solid oxide fuel cell stack assembly according tothe present disclosure.

FIG. 3 depicts a schematic side section view taken through anon-limiting exemplary fuel reformer module according to the disclosure.

FIG. 4 depicts a schematic side section view of a non-limiting exemplarycatalyzing body embodiment of a SOFC system according to the disclosure.

FIG. 4A is a schematic diagram depicting surface area of the reactorbase wall that is available to absorb thermal energy being radiated fromcatalyst fuel passages according to the present disclosure.

FIG. 5 depicts a schematic top section view taken through a non-limitingexemplary cathode chamber according to the disclosure.

FIG. 6 depicts a bottom schematic section view taken through anon-limiting exemplary fuel reformer module according to the disclosure.

FIG. 7 depicts a schematic side section view taken through anon-limiting exemplary solid oxide fuel cell stack assembly according tothe present disclosure.

FIG. 8 depicts a schematic representation of a further non-limitingexemplary embodiment of a Solid Oxide Fuel Cell (SOFC) system thatincludes a fuel and air input system according to the presentdisclosure.

FIG. 9 depicts a first exemplary, non-limiting thermally conductiveelement embodiment, in thermally conductive contact with a catalyzingbody according to the present disclosure.

FIG. 10 depicts a second exemplary, non-limiting thermally conductiveelement embodiment, in thermally conductive contact with a catalyzingbody according to the present disclosure.

FIG. 11 depicts a third exemplary, non-limiting thermally conductiveelement embodiment, in thermally conductive contact with a catalyzingbody according to the present disclosure.

FIG. 12 depicts a fourth exemplary, non-limiting thermally conductiveelement embodiment, in thermally conductive contact with a catalyzingbody according to the present disclosure.

FIG. 13A depicts an isometric top view of a fifth exemplary,non-limiting embodiment depicting a cylindrical catalyzing body formedwith a central longitudinal passage provided to receive a thermallyconductive element therein according to the present disclosure.

FIG. 13B depicts a section view taken through a longitudinal axis of thecylindrical catalyzing body formed with a central longitudinal passageand depicting a solid cylindrical thermally conductive element thereinaccording to the present disclosure.

FIG. 14 depicts an isometric top view of a sixth exemplary, non-limitingthermally conductive element embodiment, in thermally conductive contactwith a catalyzing body formed as a solid non-porous ceramic foammaterial formed with interconnecting open cells distributed through thesolid ceramic foam structure according to the present disclosure.

FIG. 15A depicts a graphic representation of O:C ratio vs T_CPOX values,% CH₄ values and % C₂Hx values.

FIG. 15B depicts a data table listing the O:C ratio vs T_CPOX values, %CH₄ values and % C₂Hx values plotted in FIG. 15A.

6 DEFINITIONS

The following definitions are used throughout, unless specificallyindicated otherwise:

TERM DEFINITION Hastelloy A group of alloys comprising predominantlymetal nickel plus molybdenum, chromium, cobalt, iron, copper, manganesetitanium, zirconium, aluminum, and tungsten in varying percentages,between zero and 20%. Hastelloy alloys are primarily used for effectivesurvival under high temperature and or high stress in moderate toseverely corrosive environments. Available from Haynes InternationalInc. of Kokomo IN, USA. Monel A group of alloys comprising up to 67%metal nickel and cobalt, up to 30% copper with between 0 and 5% iron,titanium, manganese, carbon, and silicon and aluminum. Monel is used forits resistance to corrosion. Available from Special Metals Corp. of NewHartford NY, USA. SOFC Solid Oxide Fuel Cell Inconel A family ofaustenitic nickel-chromium alloys comprising nickel 40-70%, chromium14-30%, iron 3-9%, manganese 0.3-1%, plus silicon, carbon, sulfur, andother elements. Inconel is used for its resistance to oxidation andcorrosion and strength over a wide range of temperatures. When heated,Inconel forms a thick stable passivating oxide layer protecting thesurface from further attack. Attractive for high temperatureapplications to reduce creep. Available from Special Metals Corp. of NewHartford NY, USA. Cermet Any of a class of heat-resistant materials madeof ceramic and sintered metal. Often formed and sintered as a ceramicoxide mixture and converted through the reduction from an oxide ceramicto the metallic phase. (NiO-YSZ →Ni-YSZ). Perovskite A ternary materialwith the general structure A^([12])B^([6])X- 3^([6]) same type ofcrystal structure as calcium titanium oxide (CaTiO₃).

7 ITEM NUMBER LIST

The following item numbers are used throughout, unless specificallyindicated otherwise.

ITEM NUMBER DESCRIPTION  100 SOFC system  105 Hot zone  110 Cold zone 115 Hot zone enclosure walls  120 Hot zone cavity  125 Anode gas  125aSpent anode gas  126 Cathode gas  126a Spent cathode gas  127 Combustionexhaust gases  127a Spent exhaust gas  130 Thermal insulation  132 Outerenclosure walls  135 Fuel cell stack  140 DC power output module  145Solid electrolyte layer  150 Solid oxide anode electrode  155 Solidoxide cathode electrode  157 Hot zone thermocouple/ temperature sensor 160 Incoming fuel  165 Fuel reformer module  167 Catalyst supportstructure  170 Incoming air  175 Recuperator module  180 Combustormodule  185 Exhaust port  190 Electronic controller  195 Cold startmodule  197 Fuel input module  198 Air input module  2000 SOFC fuel cellstack assembly  2005 SOFC fuel cell stack  2010 Cathode chamber  2015Longitudinal cylindrical side wall  2016 Disk shaped bottom end wall 2017 Disk shaped top end wall  2020 Fuel reformer module  2025 Incomingfuel air mixture  2026 Spent cathode gas  2027 Reformed fuel/syngas 2028 Spent fuel  2045 Fuel input conduit  2055 Fuel inlet manifold 2060 Longitudinal axis  2080 Tubular fuel cells  2082 Disk shaped toptube support wall  2084 Disk shaped bottom tube support wall  2086 Tubeholding flange  2115 Anode gas flow  2135 Combustion chamber  2145Cathode feed tube  2150 Combustor exit port  2155 Air gap  2165 Systemexit port  2200 Incoming air  2205 Air input port  2210 Recuperatorchamber  2212 Flow barrier  2214 Disk shaped separator wall  2230Recuperator input ports  2235 Recuperator output port  2240 Air exitports  2245 Cathode chamber exit port  2300 Cold start combustionchamber  2302 Cold start exit port  2304 Fuel inlet  2306 Ignitor  2510Intermediate cylindrical sidewall  2511 Disk shaped intermediate bottomend wall  2512 Thermal insulation  2513 Disk shaped intermediate top endwall  2514 Outer cylindrical sidewall  2516 Disk shaped outer top wall 2518 Disk shaped outer bottom wall  2830 Fuel supply valve powerconduit  3000 Fuel reformer system  3005 Cylindrical fuel chamber  3010Annular perimeter wall  3015 Reactor shield base wall  3017 Fuel chambercap  3020 Fuel reformer module  3025 Incoming fuel air mixture  3030Cylindrical catalyzing body  3032/3033 Catalyzing body input end  3034Catalyzing body output end  3035 Cylindrical catalyzing cavity  3040Fuel reactor body  3055 Fuel inlet manifold  3060 Annular enclosure wall 3065 Catalyzing body support flange  3070 Circular aperture  3075 Firstannular washer  3080 Annular thermally insulting element  3085 Catalystfuel passage  3088 Catalyst fuel passage (larger square)  3090 Catalystlayer  3095 Base wall fuel passages  3100 Heat dissipating flange  3102Disk shaped outer enclosure top end flange  3105 Annular seal plate 3110 O-ring seal element  3115 O-ring seal element  3120 Fasteners 3125 Array of fuel passages  3130 Air moving element  3135 Temperaturesensing element  3140 Communication pathway  5000 SOFC system  5002Cathode chamber  5010 Circumferential edge  5015 Inner shaded area  5020Outer shaded area  5025 Cathode feed tube  5030 Longitudinal centralaxis  5035 Inner circular pattern  5040 Tubular fuel cell  5045 Outercircular pattern  7000 Fuel Reformer System  7005 Fuel chamber  7010Annular perimeter wall  7015 Reactor shield base wall  7020 Fuelreformer module  7035 Cylindrical catalyzing cavity  7040 Fuel reactorbody  7045 Fuel conduit  7060 Annular enclosure wall  7102 Outerenclosure top end flange  7105 Annular seal plate  7110 O-ring sealelement  7135 External temperature sensor  7140 Communication pathway 7610 Fuel supply valve  7666 Fuel supply valve communication channel 7830 Power conduit  7860 Thermal fuse  8000 Solid Oxide Fuel Cell(SOFC) system  8005 Fuel/oxidant input control module  8010 Oxidantsupply source  8015 Mixing chamber  8017 Oxidant input conduit  8020Hydrocarbon fuel supply source  8022 Fuel input conduit  8025 Oxidantflow modulator  8030 First thermal sensor  8031 First temperature signal 8035 Hydrocarbon fuel flow modulator  8040 Second thermal sensor  8041Second temperature signal  8045 Cathode air or other oxidant source 8050 Cathode air flow modulator  8055 Cathode air input conduit  9005Prismatic rod  9010 External surface of the catalyzing body  9015Longitudinal axis of the prismatic rod  9020 Longitudinal axis of thecatalyzing body  9025 Through hole or blind hole 10005 Nearly horizontalcylindrical segment 10010 External surface of the catalyzing body 10015Longitudinal axis of the nearly horizontal cylindrical segment 10020Longitudinal axis of the cylindrical catalyzing body 10025 Through holeor blind hole 11005 Hollow cylinder 11010 External surface of thecatalyzing body 11015 Longitudinal axis of the hollow cylinder 11020Longitudinal axis of the catalyzing body 12005 Spiral portion of ahollow cylinder 12010 External surface of the catalyzing body 12015Longitudinal axis of the spiral portion of a hollow cylinder 12020Longitudinal axis of the catalyzing body 13005 Thermally conductiveelement 13007 Central cavity 13010 Circumferential external surface13020 Central longitudinal axis of the cylindrical catalyzing body 13025Through hole or blind hole 13030 Cylindrical catalyzing body 13032 Inputend of the cylindrical catalyzing body 13034 Output end of thecylindrical catalyzing body 14010 Circumferential external surface 14020Longitudinal axis of the cylindrical catalyzing body 14030 Cylindricalcatalyzing body 14031 Open cells 14032 Input end 14034 Output end  1500Calibration data graph  1505 Calibration data table  1510 Linear plot 1515 Non-linear plot  1520 Plot that is not clearly linear ornon-linear  1530 Set point values

DETAILED DESCRIPTION

8.1 Solid Oxide Fuel Cell System

Referring to FIG. 1, a schematic diagram of a first exemplarynon-limiting embodiment of the present disclosure depicts a Solid OxideFuel Cell (SOFC) system (100). The system (100) includes a hot zone(105) enclosed within hot zone enclosure walls (115) which in thepresent embodiment enclose a cylindrical hot zone cavity (120). The hotzone enclosure walls (115) are further enclosed by a layer of thermalinsulation (130) which is further enclosed by outer enclosure walls(132). The hot zone enclosure walls (115) and the outer enclosure walls(132) each include a separate cylindrical side wall with each sidewallmechanically interfaced with a different pair of opposing disk shapedend walls described further below.

The hot zone enclosure walls (115) enclose a fuel cell stack (135). Thefuel cell stack (135) includes at least one SOFC fuel cell butpreferably includes a plurality of SOFC fuel cells each electricallyinterconnected in series or in parallel with a DC power output module(140). The DC power output module receives electrical power generated bythe fuel cell stack and delivers output power to an external power load,(not shown). Each fuel cell comprises a solid oxide cathode electrode(155) which is oriented for exposure to cathode gas present inside thehot zone cavity (120). The hot zone cavity (120) is filled with acathode gas that at least comprises oxygen, e.g. air, (126) duringoperation and the cathode gas in the hot zone cavity (120) chemicallyreacts with surfaces of the solid oxide cathode electrode (155). Eachfuel cell further comprises a solid oxide anode electrode (150) which isnot exposed to the hot zone cavity (120) or to the cathode gas containedtherein but instead is oriented for exposure to an anode gas (reformedfuel) (125) such that during operation the anode gas is passed over thesolid oxide anode electrode (150) in order to chemically react with thesolid oxide anode electrode (150). The SOFC fuel cell further comprisesa solid electrolyte layer (145) disposed to separate the solid oxidecathode electrode (155) from the solid oxide anode electrode (150). Thesolid electrolyte layer (145) is an oxygen ion conducting layer providedas an ion exchange medium for ion exchange between the solid oxide anodeelectrode (150) and the solid oxide cathode electrode (155).

The fuel cell stack (135) is maintained at a high operating temperature(e.g. ranging from 350 to 1200° C.), depending on the composition of thesolid material layers of the fuel cell stack and the characteristics ofthe anode and cathode gases. A preferred operating temperature isselected to support efficient electrochemical energy generation.Electrical energy is generated by the fuel cell stack (135) when anodegas (125) comprising hydrogen is reacted with the solid oxide anodeelectrode (150) and cathode gas (126) comprising oxygen is reacted withthe solid oxide cathode electrode (155).

The hot zone (105) further encloses a combustor module (180), ortail-gas combustor, which comprises a combustion chamber configured toreceive spent anode gas (125 a) and spent cathode gas (126 a) after eachof the spent anode gas and the spent cathode gas has reacted with thecorresponding solid oxide anode electrode (150) and solid oxide cathodeelectrode (155). Upon mixing in the combustor module (180) the spentanode gas (125 a) and the spent cathode gas (126 a) are combusted.Thermal energy generated by combustion taking place inside thecombustion module (180) is used to heat the hot zone enclosure walls(115) as well as the hot zone cavity (120).

The hot zone cavity (120) further encloses a recuperator module (175).The recuperator module (175) is in fluid communication with thecombustor module (180) and receives combustion exhaust gases (127)exiting therefrom. The combustion exhaust gases (127) pass through therecuperator module (175) and transfer thermal energy therefrom toincoming air (170) when each of the combustion exhaust gases (127) andthe incoming air (170) pass through separate gas conduits of a gascounter flow heat exchanger (not shown). Thereafter, spent combustionexhaust gas (127 a) exits the recuperator module (175) and is deliveredout of the hot zone through an exhaust port (185). The incoming air(170) after exiting from the recuperator module (175) comprises thecathode gas (126) which is delivered into the hot zone cavity (120).

The system cold zone (110) includes a fuel input module (197). Varioushydrocarbon fuels such as propane, methane, or kerosene, and othersuitable fuels, are received into the fuel input module (197) fromvarious fuel sources (not shown). The fuel input module (197) isoperable to modulate incoming fuel (160) delivered from the fuel sourceand deliver a desired volume or mass flow rate of incoming fuel (160) tothe fuel reformer module (165). The fuel reformer (165) is operable toreform the fuel in a manner that makes the incoming fuel more suitablefor the desired chemical reaction with the solid oxide anode electrode(150).

The incoming fuel (160) comprises a liquid or gaseous hydrocarboncompound from which hydrogen can be extracted. The incoming fuel (160)may be mixed with air and may be atomized or otherwise vaporized. Thefuel reformer module (165) of the present disclosure comprises aCatalytic Partial Oxidation (CPOX) reactor which provides a catalystsupport structure (167) having some of its surfaces coated by acatalytic layer, described below. As the incoming fuel is passed overthe catalyst layer, the fuel is combusted or partially combusted insidethe catalyst support structure (167). The heat generated by thecombustion reforms the incoming fuel (160) into hydrogen gas (H.sub.2)and carbon monoxide gas (CO). The reformed fuel exits the fuel reformermodule (165) as anode gas (125) which is reacted with the solid oxideanode electrode (150) of each fuel cell in the SOFC fuel cell stack(135).

The system cold zone (110) includes an air input module (198) forincoming air (170) or another oxygen rich source gas into therecuperator module (175). Air or any other oxygen rich source gas isreceived into the air input module (198) from various air sources, (notshown), or the air comprises room air which is pumped into therecuperator module (175) by a fan. The air input module (198) isoperable to modulate air flow into the recuperator module (175). Therecuperator module (175) heats the incoming air (170) with combustionexhaust gases (127) by passing the combustion exhaust gases through agas counter flow heat exchanger (not shown). The heated air exits therecuperator as the cathode gas (126).

The system cold zone (110) includes an electronic controller (190) inelectrical communication with the fuel input module (197) and the airinput module (198). The electronic controller (190) includes a digitaldata processor and associated digital data memory with various operatingprograms and or digital logic control elements operating thereon tomanage operation of the SOFC system (100). The electronic controller(190) is in electrical communication with the DC power output module(140) to monitor and modulate DC power output to a load. The electroniccontroller is also in electronic communication with the fuel inputmodule (197) to monitor and modulate incoming fuel (160) and further isin electronic communication with the air input module (198) to monitorand modulate incoming air (170) and further is in electroniccommunication with the at least one temperature sensor (157) to monitorthe temperature of one or more surfaces of the hot zone enclosure walls(115), the outer enclosure walls (132), the fuel reformer module (165)and other surfaces as may be required to monitor temperature of varioussurfaces of the SOFC system (100).

Each of the fuel input module (197) and the air input module (198) mayinclude one or more gas pressure regulators, gas flow actuator valves,mass or volume gas flow rate controllers, and or mass flow rate sensors,or the like, gas pressure sensors, or the like, and temperature sensors,or the like, each operable by or otherwise in electrical communicationwith the electronic controller (190) to modulate incoming fuel (160)into the fuel reformer module (165) or incoming air (170) into therecuperator module (175). More specifically the fuel input module (197)in cooperation with the electronic controller (190) is operable toregulate input fuel pressure, to variably regulate incoming fuel mass orvolume flow rates and to stop incoming fuel (160) from entering the SOFCsystem (100) as required. Similarly, the air input module (198) incooperation with the electronic controller (190) may also be operable toregulate input air pressure, to variably regulate incoming air mass orvolume flow rates and to stop incoming air (170) from entering the SOFCsystem (100) as required. In some operating environments the air inputmodule (198) may comprise a simple fan running at constant angularvelocity without any further air input control sensors or elements.

According to the present disclosure the fuel reformer module (165) isconfigured to cause an exothermic reaction between the incoming fuel(160) and catalyst layers provided on surfaces of the ceramic catalystsupport structure (167) in order to reform the fuel into hydrogen gas(H.sub.2) and carbon monoxide (CO). Further, according to the presentdisclosure an improved fuel reformer module (165) comprises a ceramiccatalyst support structure (167) comprising a plurality of longitudinalfuel flow passages, described below, with each longitudinal fuel flowpassage being coated on internal surfaces thereof with a catalyst layer.In addition, the fuel reformer module (165) is configured to preventauto ignition of unprocessed fuels entering the ceramic catalyst supportstructure (167) in part by providing the longitudinal fuel flow passageas a means of transferring thermal energy generated by the exothermicreaction taking place inside the ceramic catalyst support structure(167) out of the ceramic catalyst support structure (167) along thelongitudinal pathways toward the incoming fuel. As can be seen in FIG.1, the fuel reformer module (165) is disposed in part between the outerenclosure walls (132) and in part outside the outer enclosure walls(132) and is further configured to provide a thermally conductivepathway that passes through the outer enclosure walls (132). Inaddition, the SOFC system (100) optionally includes one or more coolingdevices (e.g. air fans, water pumps, or the like) to cool portions ofthe fuel reformer module (165) that are disposed outside the outerenclosure walls (132).

The SOFC system (100) may optionally include a cold start module (195).The cold start module (195) is configured to receive and combust aportion of the incoming fuel (160) which is redirected into the coldstart module (195). Operation of the cold start module (195) isinitiated by the electronic controller (190) when the temperature of theincoming fuel (160) or the temperature of the hot zone enclosure walls(115) or the temperature of the fuel cell stack (135) is below a desiredoperating or reaction temperature. In operation, a portion of theincoming fuel (160) is diverted to a combustion chamber associated withthe cold start module (195). A controllable fuel igniter is providedinside a combustion chamber of the cold start module (195) and fuelinside the combustion chamber is ignited and combusted to heat theincoming fuel (160), the fuel reformer module (165) and the hot zoneenclosure walls (115) during a cold start. Once the SOFC system (100)reaches its desired operating temperature, operation of the cold startmodule (195) is terminated.

During operation, the electronic controller (190) is in communicationwith other electronic elements such as one or more cooling fans, one ormore electrically operable gas flow actuator valves, gas flow ratedetectors, and or gas modulators, associated with the fuel input module(197), the air input module (198) and electrical power output detectors,or the like, and other elements as may be required to control variousoperating parameters of the SOFC (100). The electronic controller (190)monitors DC current/power output as well as temperature measured by oneor more thermocouples, or the like, and further operates to vary themass flow rate of incoming fuel and optionally of incoming air as ameans of increasing or decreasing DC current/power output.

8.2 Solid Oxide Fuel Cell Stack Side Section

Turning now to FIG. 2, a second non-limiting exemplary embodiment of animproved SOFC fuel cell stack assembly (2000) according to the presentdisclosure is shown in side section view. The SOFC fuel cell stackassembly (2000) includes a SOFC fuel cell stack (2005) comprising aplurality of tubular fuel cells (2080) each longitudinally extendedalong a substantially cylindrical hot zone cavity or cathode chamber(2010).

Turning now to FIG. 2, a second non-limiting exemplary embodiment of animproved SOFC fuel cell stack assembly (2000) according to the presentdisclosure is shown in side section view. The SOFC fuel cell stackassembly (2000) includes a SOFC fuel cell stack (2005) comprising aplurality of tubular fuel cells (2080) each longitudinally extendedalong a substantially cylindrical hot zone cavity or cathode chamber(2010).

In the present example embodiment, the disk shaped bottom end wall(2016) also forms a bottom wall of a recuperator chamber (2210). Asdescribed above the recuperator chamber (2210) is provided to heatincoming air (2200) entering the fuel cell stack assembly through acathode feed tube (2145). The incoming air (2200), or cathode gas, flowsinto the recuperator chamber (2210) through recuperator input ports(2230) and out of the recuperator chamber (2010) returning back to thecathode feed tube (2145) through recuperator output ports (2235). One ora plurality the recuperator input ports (2230) and the recuperatoroutput port (2235) may be disposed around the circumference of thecathode feed tube (2145). A flow barrier (2212) directs air flow towardperipheral walls of the recuperator chamber (2210) thereby increasingthermal energy exchange between air passing through the recuperatorchamber and its peripheral walls. The recuperator chamber (2210) isbounded on a top side thereof by a disk shaped separator wall (2214)disposed between a combustion chamber (2135) and the recuperator chamber(2210). The disk shaped separator wall (2214) is configured to absorbthermal energy as spent anode and spent cathode gas is combusted insidethe combustion chamber (2135) such that the absorbed thermal energy isreemitted into the recuperator chamber (2210).

An intermediate cylindrical enclosure surrounds the hot zone enclosurewalls. The intermediate cylindrical enclosure is bounded by an openended longitudinal intermediate cylindrical side wall (2510) thatmechanically interfaces with a disk shaped intermediate bottom end wall(2511) and an opposing disk shaped intermediate top end wall (2513). Theintermediate cylindrical enclosure is sized to form an air gap (2155)substantially surrounding the longitudinal cylindrical side wall (2015)and the disk shaped top end wall (2017). The air gap (2155) provides afluid flow passage proximate to portions of the hot zone enclosure wallsand the fluid passage is in fluid communication with a system exit port(2165). The air gap (2155) is further in fluid communication with thecombustion chamber (2135) through one or more combustor exit ports(2150) and is in fluid communication with a cold start combustionchamber (2300) through one or more cold start exit ports (2302).Accordingly exhaust gas exiting each the combustion chamber (2135) andthe cold start combustion chamber (2300) flows over outside surfaces ofthe hot zone enclosure walls before exiting the fuel cell stack assembly(2000) through the system exit port (2165). In one non-limiting exampleembodiment the dimension of the air gap (2155) from an exterior surfaceof wall (2015) to an interior surface of wall (2510) ranges from 1 to 4mm. The intermediate cylindrical enclosure also encloses a cold startcombustion chamber (2300) further described below.

Each of the intermediate enclosure walls (2510, 2511, and 2513) compriseHastelloy, a Cobalt-Nickel-Chromium-Tungsten alloy that combinesexcellent high temperature strength with very good resistance tooxidizing environments up to 2000° F. (1095° C.). Other metal alloys arealso suitable including Monel, which is a group of alloys comprising upto 67% metal nickel and about 30% copper with smaller amounts of iron,manganese, carbon, and silicon. In any event the intermediate enclosurewalls (2510, 2511, and 2513) are preferably formed from a metal alloythat has a coefficient of thermal conductivity of less than about 25.0W/m° K at the operating temperature of the hot zone. This much lowercoefficient of thermal conductivity of the intermediate enclosure wallsas compared with the thermal conductivity of the hot zone enclosurewalls causes a much slower conductive heat flow rate from one area ofthe intermediate enclosure walls to another as compared with the heatflow rate of the hot zone enclosure walls which are formed from a metalalloy having much higher, e.g. at least 4 times greater, coefficient ofthermal conductivity. Thus, according to one aspect of the presentdisclosure the intermediate enclosure walls (2510, 2511, and 2513) areformed as a second thermally conductive pathway having a slower rate ofthermally conducted heat transfer. One other embodiments theintermediate enclose walls (2510, 2511, and 2513) may comprise steel orother metal alloys that may have a coefficient of thermal conductivityof less than about 50.0 W/m° K without deviating from the presentdisclosure.

An outer cylindrical enclosure surrounds the intermediate cylindricalenclosure. The outer enclosure is bounded by an open ended outercylindrical side wall (2514) that mechanically interfaces with a diskshaped outer bottom wall (2518) and an opposing disk shaped outer topwall (2516). Each of the walls (2514, 2518, and 2516) preferablycomprises aluminum or an aluminum alloy preferably having a coefficientof thermal conductivity above 140 W/m° K to support rapid thermal energyconduction in order to provide a substantially homogeneous temperatureof the outer cylindrical enclosure during operation. A layer of thermalinsulation (2512) is disposed between outside surfaces of theintermediate enclosure walls and the inside surfaces of outer enclosurewalls and the layer of thermal insulation (2512) impedes thermal energybeing radiated across the air gap (2155) or being carried through theair gap by exhaust gases exiting the SOFC system from reaching surfacesof the outer cylindrical side wall (2514) and the disk shaped outerbottom wall (2518). Preferably, the layer of thermal insulation (2512)is constructed to ensure that surfaces of the outer cylindrical sidewall (2514) and the disk shaped outer bottom wall (2518) remain withinoperational parameters, e.g. the layer of thermal insulation (2512) isconfigured to prevent the temperature of the outer cylindrical side wall(2514) and the disk shaped outer bottom wall (2518) from reaching morethan about 110° C. Thus, according to one aspect of the presentdisclosure the outer enclosure walls (2514, 2518, and 2516) are formedas a third thermally conductive pathway.

A plurality of tubular fuel cells (2080) also known as fuel rods or rodsare longitudinally supported inside the cathode chamber (2010) betweendisk shaped top tube support wall (2082) and opposing disk shaped bottomtube support wall (2084). Each tubular fuel cell (2080) comprises asolid oxide anode electrode support structure that forms the insidediameter of the tube. A solid ceramic electrolyte layer is formed overthe outside diameter of the solid oxide anode electrode support layerand a solid oxide cathode electrode layer is formed over the outsidediameter of the solid electrolyte layer. Each tubular fuel cell (2080)is open at both ends thereof and provides a cylindrical fluid conduitfor anode gas, also referred to herein as reformed fuel or syngas, toflow through. A plurality of tube holding flanges (2086) are optionallyprovided to support tube ends with respect to the top tube support walls(2082) and the bottom tubular support wall (2084). Each tube holdingflange (2086) also includes an electrically conductive terminalelectrically interfaced to the DC power output module (140).

The solid anode electrode used to form the support layer of each tubularfuel cell (2080) may comprise a cermet material such as nickel and dopedzirconia, nickel and doped ceria, or copper and ceria. Alternately thesolid anode electrode may comprise a perovskite such asSr2Mg1-xMnxMoO6-δ or La 0.75Sr0.25Cr0.5Mn0.5O3-δ. In either case theinside surface of each of the tubular fuel cells (2080) comprises thesolid oxide anode electrode and anode gas flow (2115) passes througheach disk shaped top tube support wall (2082) such that only anode gasflow (2115) enters each of the tubular fuel cells (2080) through a fuelinlet manifold (2055) to react with the solid anode electrode.

The solid oxide cathode electrode may comprise any one of LanthanumStrontium Cobalt Oxide (LSC), Lanthanum Strontium Cobalt Iron Oxide(LSCF), or Lanthanum Strontium Manganite (LSM). The solid oxide cathodeelectrode forms an outside surface of each tubular fuel cell (2080). Asthe cathode chamber (2010) is filled with the incoming air (2200) (i.e.cathode gas), the cathode gas reacts with the solid oxide cathodeelectrode formed on the outside surface of each tubular fuel cell(2080).

The electrolyte layer is disposed between the anode layer and thecathode layer. The preferred electrolyte layer comprises an ionconducting ceramic medium and preferably comprises an oxygen ionconductor such as yttrian doped zirconia or gadolinium doped ceria.Alternately, the electrolyte layer is a proton conducting ceramic suchas barium cerates or barium zirconates. Ideally, the electrolyte layeris formed with sufficient thickness so as to provide a near hermeticbarrier between the anode electrode and the cathode electrode to preventanode and cathode gas from crossing the electrolyte layer.

The improved SOFC fuel cell stack assembly (2000) optionally includes acold start combustion chamber (2300). The cold start combustion chamber(2300) is housed within the intermediate chamber walls and is bounded bythe intermediate longitudinal cylindrical side wall (2510), theintermediate top wall (2513) and the disk shaped top end wall (2017) ofthe cathode chamber. The cold start combustion chamber (2300) forms anannular chamber volume that partly surrounds the fuel reformer module(2020). When starting the SOFC system from a cold start, a portion ofthe incoming fuel air mixture (2025) is diverted to the cold startchamber (2300) through a fuel inlet (2304) and ignited by an igniter(2306). Thus, during a cold start a portion of the incoming fuel airmixture (2025) is combusted in the cold start combustion chamber (2300).The thermal energy generated by combustion in the cold start combustionchamber (2300) is radiated into the surrounding walls thereof, whichincludes the disk shaped top end wall (2017), that is specificallyconfigured with a copper core provided to rapidly absorb thermal energy.Moreover, the disk shaped top end wall (2017) is part of the hot zoneenclosure walls surrounding the cathode chamber (2010) which form thefirst thermally conductive pathway. Once absorbed by the disk shaped topend wall (2017) thermal energy is rapidly conducted through the hot zoneenclosure walls which all comprise highly thermally conductivematerials. Exhaust from combustion taking place inside the cold startchamber (2300) exits the chamber through exhaust ports (2302) and passesthrough the air gap (2155) to the system exit port (2165). During thepassage through the air gap (2155) the combustion exhaust transfersthermal energy to the hot zone enclosure walls (2015) and (2016) byradiation and convection to further aid in heating the hot zoneenclosure walls to a desired steady state operating temperature.

The incoming fuel air mixture (2025) enters the improved SOFC fuel cellstack assembly (2000) through a fuel reformer module (2020). In thepresent preferred embodiment, the fuel reformer is a Catalytic PartialOxidation (CPOX) reactor. The fuel reformer module (2020) receives theincoming fuel air mixture (2025) through the fuel input conduit (2045)and reforms the incoming fuel air mixture (2025) to provide reformedfuel or syngas (2027) which is used as the anode gas to react with thesolid oxide anode electrode formed on the inside wall of each of thetubular fuel cells (2080). The reformed fuel or syngas (2027) exits fromthe fuel reformer module (2020) and enters a fuel inlet manifold (2055).The fuel inlet manifold (2055) is configured to distribute anode gasinto a top or input end of each of the plurality of tubular fuel cells(2080). At the bottom or output end of each tubular fuel cell (2080),spent fuel (2028) comprising hydrogen depleted anode gas exits thetubular fuel cell to the combustion chamber (2135) where is it mixedwith spent cathode gas (2026) or oxygen depleted air and combusted.

Incoming air (2200), or cathode gas, shown by dashed lines, enters theimproved SOFC fuel cell stack assembly (2000) through the cathode feedtube (2145), passes through the recuperator chamber (2210) where it isheated by surfaces thereof and then reenters the cathode feed tubethrough recuperator output ports (2235). The heated air then passesthrough the combustion chamber (2135) while flowing through the cathodefeed tube (2145) where the air is further heated by thermal energy beinggenerated by combustion and being transferred to and through the wall ofthe cathode feed tube (2145) before entering the cathode chamber (2010).A plurality of air exit ports (2240) pass through the cathode feed tube(2145), inside the cathode chamber (2010) and the heated air enters thecathode chamber (2010) through the air exit ports (2240). Once insidethe cathode chamber, the heated air or cathode gas reacts with the solidoxide cathode electrode formed on the outside surface of each tubularfuel cell (2080). Spent cathode gas (2026) exits the cathode chamberthrough cathode chamber exit ports (2245) to the combustion chamber(2135) where it is mixed with spent anode gas (2028) and combusted.Exhaust gas exits from the combustion chamber (2135) to the air gap(2155) through the combustor exit ports (2150) to heat the walls of therecuperator chamber (2210) as the exhaust gas flows toward the systemexit port (2165).

8.3 Solid Oxide Fuel Cell Stack Top Section View

The schematic diagram of FIG. 2 depicts a schematic side section view ofan improved SOFC fuel cell stack assembly (2000) that shows only twotubular fuel cells (2080) to simplicity the description. However, apreferred stack comprises more than two tubular fuel cells (2080) withthe fuel cells arranged within the cathode chamber (2005) in a mannerthat provides efficient use of space, promotes efficient gas flowpatterns and provides the desired power output at the desired voltage.

Referring now to FIG. 5 the figure depicts a non-limiting exemplaryschematic top section view taken through a non-limiting exemplarycathode chamber of an improved SOFC stack (5000) of one example of thepresent disclosure. The cathode chamber (5002) is bounded by an openended longitudinal cylindrical side wall, e.g. longitudinal cylindricalside wall (2015) shown in FIG. 2 which defines a circumferential edge(5010). The inner shaded area (5015) represents the longitudinalintermediate cylindrical side wall (2510) and the air gap (2155) shownin FIG. 2. The outer shaded area (5020) represents the layer of thermalinsulation (2512) and the outer cylindrical side wall (2514) shown inFIG. 2.

A cathode feed tube (5025) is positioned at the center of the cathodechamber (5002) to distribute cathode gas into the cathode chamberthrough a plurality of radially disposed air exit ports, e.g. (2240)shown in FIG. 2. A longitudinal central axis (5030) centers the cathodefeed tube (5025) and the circumferential edge (5010).

The improved SOFC stack (5000) includes a plurality of substantiallyidentical tubular fuel cells (5040) each comprising a solid oxide anodeelectrode that structurally forms the inside diameter of each tubularfuel cell (5040) and with a solid oxide cathode electrode formed on theoutside diameter of each tubular fuel cell (5040). A first plurality oftubular fuels is arranged in an inner circular pattern (5035) with thecenter of each of the first plurality of tubular fuels at the sameradial distance from the longitudinal central axis (5030) as shown bythe inner circular pattern (5035). The inner circular pattern (5035) maybe a symmetrical circular pattern wherein the inner tubular fuel cellsare equally spaced apart around the inner circular pattern (5035) or thefirst plurality of tubular fuel cells may be positioned around the innercircular pattern (5035) with unequal angular distribution or angularseparation.

A second plurality of tubular fuel cells is arranged in an outercircular pattern (5045) with the center of each of the second pluralityof tubular fuel cells at the same radial distance from the longitudinalcentral axis (5030) as shown by the outer circular pattern (5045). Theouter circular pattern (5045) may be a symmetrical circular patternwherein the second plurality of fuel cells is equally spaced apartaround the outer circular pattern (5045) or the second plurality of fuelcells may be positioned around the outer circular pattern (5045) withunequal angular distribution of angular separation. In the presentexample embodiment, the total number of fuel cells is twenty-two (22).Other patterns of fuel cell distribution with other total number of fuelcells are usable without deviating from the present disclosure.

8.4 Improved CPOX Fuel Reformer

Referring now to FIGS. 2-4 a fuel reformer system (3000) according tothe present disclosure is shown in a schematic side section view in FIG.3 and partially in exploded side section view in FIGS. 4 and 4A. Thefuel reformer system (3000) comprises a fuel reformer module (3020)mounted above a fuel inlet manifold (3055). The fuel reformer module(3020) includes a fuel reactor body (3040) configured to receive anincoming fuel air mixture (3025), i.e. unreformed fuel, into acylindrical fuel chamber (3005) which is bounded by an annular perimeterwall (3010), by a reactor shield base wall (3015) and a by a fuelchamber cap (3017). In a preferred embodiment, fuel chamber cap (3017)is welded to the annular side wall (3010). The fuel reformer system(3000) further includes a cylindrical catalyzing body (3030). Each ofthe fuel reactor body (3040) and the cylindrical catalyzing body (3030)is installed into a cylindrical catalyzing cavity (3035) with thecylindrical catalyzing body (3030) positioned just above the fuel inletmanifold (3055) and the fuel reactor body (3040) position just above thecylindrical catalyzing body (3030). Each of the fuel reactor body (3040)and the cylindrical catalyzing body (3030) is configured to providefluid communication between the cylindrical fuel chamber (3005) and thefuel inlet manifold (3055).

A preferred reactor body material has a coefficient of thermalconductivity greater than 100 W/m° K and sufficient thermal mass ormaterial volume to rapidly conduct thermal energy away from theinterface between the fuel reactor body (3040) and the catalyzing body(3030). A preferred catalyzing body material comprises a ceramicsubstrate configured to provide reliable operation in the elevatedtemperature, and chemically harsh environment of the CPOX reaction.Typically ceramic materials have a coefficient of thermal conductivityof less than about 40 W/m° K but often less than about 10 W/m° K whichreduces the rate of thermal conduction from one region of the catalyzingbody to another.

In the present non-limiting exemplary embodiment, the cylindricalcatalyzing cavity (3035) has a side wall formed by an inside diameter ofthe annular enclosure wall (3060) which is formed with its longitudinalcentral axis coaxial with the central longitudinal axis (2060), shown inFIG. 2. The cylindrical catalyzing cavity (3035) includes two open endseach forming a circular aperture with one circular aperture passingthrough the disk shaped outer top wall (2516) of the outer enclosure andthe other circular aperture passing through the disk shaped top end wall(2017) of the hot zone enclosure.

In a preferred embodiment the annular enclosure wall (3060) is formed tobe less thermally conductive that the fuel reactor body (3040) todiscourage thermal conduction between the annular enclosure wall (3060)and the fuel reactor body (3040). In a preferred embodiment, the annularenclosure wall (3060) comprises Hastelloy or Monel which each have ahigh nickel content to resist oxidation damage and which each havesuitable service temperatures ratings, e.g. exceeding 400° C., and whicheach have a coefficient of thermal conductivity of less than about 25.0W/m° K. Additionally, the annular enclosure wall (3060) is thin walled,e.g. between 0.02 and 0.1 inches thick to further disclosure thermalconduction there through.

The annular enclosure wall (3060) is thermally conductively connected tothe disk shaped top end wall (2017) at its lower open end which is partof the hot zone enclosure walls defined above as the first thermallyconductive pathway. The annular enclosure wall is thermally conductivelyconnected to the disk shaped outer top wall (2516) at its top open endwhich is part of the outer enclosure walls defined above as the thirdthermally conductive pathway. The annular enclosure wall (3060) isthermally conductively connected to the intermediate top wall (2513)between its top and bottom open ends and the intermediate top wall ispart of the intermediate enclosure walls defined above as the secondthermally conductive pathway. Thus, according to one aspect of thepresent disclosure the annular enclosure wall (3060) is formed as afourth thermally conductive pathway that is thermally conductivelyconnected with each of the first thermally conductive pathway, thesecond thermally conductive pathway and the third thermally conductivepathway.

A catalyzing body support flange (3065) extends from or is formed by thedisk shaped top end wall (2017). The catalyzing body support flange(3065) is sized to define a diameter of a circular aperture (3070) whichis small enough to prevent the cylindrical catalyzing body (3030) frompassing through the circular aperture (3070). A first annular washer(3075) is disposed between the catalyzing body support flange (3065) anda bottom surface of the cylindrical catalyzing body (3030). The firstannular washer (3075) provides a gas seal between the cylindricalcatalyzing cavity (3035) when a longitudinal downward pressure isapplied to the cylindrical catalyzing body (3030). Additionally, thefirst annular washer (3075) is configured as a thermal insulator tothermally isolate the catalyzing body support flange (3065) from thedisk shaped top end wall (2017). Preferably, first annular washer (3075)comprises alumina formed with sufficient thickness and with appropriateouter edge diameter dimension to provide the desired gas sealing andthermal insulating properties. More generally, the first annular washer(3075) preferably comprises a very low thermal conductivity non-porousmaterial, e.g. having a coefficient of thermal conductivity of less than40 W/m° K, which includes most ceramic materials.

A diameter of the cylindrical catalyzing cavity (3035) is sized toreceive an annular thermally insulating element (3080) into thecylindrical catalyzing cavity (3035) surrounding the cylindricalcatalyzing body (3030). The annular thermally insulating element (3080)is provided to thermally isolate the cylindrical catalyzing body (3030)from the annular enclosure wall (3060). Additionally, the annularinsulating element (3080) is configured to precisely center thecylindrical catalyzing body (3030) with respect to a centrallongitudinal axis of the cylindrical catalyzing cavity (3035) and may befurther configured to angularly orient the cylindrical catalyzing body(3030) for precise angular alignment with one or more features of thefuel reactor body (3040). Both the first annular washer (3075) and theannular insulating element (3080) are provided to prevent thermalconduction from the enclosure walls, e.g. the annular enclosure wall(3060) and the top end wall (2017), to the catalyzing body (3030) whichis preferably operating with a higher temperature than the cylindricalcatalyzing body.

The cylindrical catalyzing body (3030) comprises a solid non-porousceramic substrate formed to include a plurality of longitudinallydisposed catalyst fuel passages (3085) each passing completely throughthe cylindrical catalyzing body (3030). Each catalyst fuel passage(3085) provides an individual fuel conduit that extends longitudinallythrough the cylindrical catalyzing body (3030). Accordingly, eachcatalyst fuel passage provides fluid communication between thecylindrical catalyzing cavity (3035) and the fuel inlet manifold (3055).Additionally, inside surfaces of each of the catalyst fuel passage(3085) are formed with a catalyst layer (3090) coated thereon. Thecatalyst layer (3090) comprises a catalyst material usable to reform theincoming fuel air mixture (3025) by catalytic partial oxidation, whichis an exothermic reaction that causes partial combustion of the fuel airmixture (3025). In the present non-limiting exemplary embodiment, apreferred catalyst layer (3090) comprises a metallic or oxide phase ofrhodium (Rh). Other suitable catalyzers usable for the catalyst layer(3090) include Pt, Pd, Cu, Ni, Ru, and Ce. The solid non-porous ceramicsubstrate used to form the cylindrical catalyzing body (3030) preferablycomprises alumina or any other non-porous material having a relativelylow coefficient of thermal conductive as compared to the coefficient ofthermal conductive of the fuel reactor body (3040). In the presentnon-limiting embodiment wherein, a ceramic substrate is used thecoefficient of thermal conductive of the catalyzing body is less than 40W/m° K.

As will be described further below the incoming fuel air mixture (3025)enters the cylindrical fuel chamber (3005), passes through the reactorshield base wall (3015), enters each of the catalyst fuel passages(3085), where it reacts with the catalyst layer (3090), and then entersthe fuel inlet manifold (3055) where it is distributed into each of thetubular fuel cells (2080).

8.5 Fuel Reactor Body

Referring now to FIGS. 2, 3, 4, and 4A, the fuel reactor body (3040) isdisposed partially within the cylindrical catalyzing cavity (3035) andpartially extending through the disk shaped outer top wall (2516) intothe cold zone such that at least a portion of the fuel reactor body(3040) is exposed to ambient air. The annular perimeter wall (3010)provides a cylindrical side wall of the cylindrical fuel chamber (3005).The fuel input conduit (2025) passes through the annular perimeter wall(3010) to deliver incoming air fuel mixture (2025/3025) into thecylindrical fuel chamber (3005). As will be recognized, other geometriesare usable to form the annular perimeter wall (3010) and fuel chamber(3005) which can have a square, rectangular or other cross-section intransverse planes thereof.

The reactor shield base wall (3015) comprises a circular bottom wall ofthe cylindrical fuel chamber (3005) that is preferably integrally formedwith the annular perimeter wall (3010). However, the reactor shield basewall (3015) and annular perimeter wall can be formed as separate partsand joined together, for example by welding, soldering, mechanicalfasteners, and or other suitable joining techniques. A plurality of basewall fuel passages (3095) each passes completely through the reactorshield base wall (3015) along a longitudinal axis, e.g. with each basewall fuel passage parallel with the central longitudinal axis (2060).Each base wall fuel passage (3095) provides a fuel conduit that extendslongitudinally through the reactor shield base wall (3015). Moreover,each base wall fuel passage (3095) is longitudinally aligned with and influid communication with a corresponding one of the plurality ofcatalyst fuel passages (3085) that pass through the cylindricalcatalyzing body (3030).

As shown in FIGS. 4 and 4A, an interface (3032) is defined by a bottomexternal surface of the reactor shield base wall (3015) and a top orinput surface of the cylindrical catalyzing body (3030). In anon-limiting exemplary embodiment one or the other or both of the twosurfaces that form the interface (3032) includes a raised feature orfeatures (3033). The raised features may include a circular ring or aplurality of discreet raised bumps, preferably three, formed at one morelocations extending from the bottom surface of the reactor shield basewall (3015) in a position that causes the raised features to contact theopposing surface at the interface (3032) in order to provide a small gapbetween the two opposing surfaces. More generally the interface (3032)is formed with a gap between the bottom surface of the reactor shieldbase wall (3115) and the top surface of the cylindrical catalyzing body(3030). The gap is provided to all allow radiant thermal energy exitingfrom each of the catalyst fuel passages to impinge onto the bottomsurface of the reactor shield base wall (3015) so that substantially allof the bottom surface of the reactor shield base wall (3015) isavailable to absorb thermal radiation impinging thereon.

At the interface (3032) each base wall fuel passage (3095) is alignedwith its corresponding catalyst fuel passages (3085) along asubstantially coaxial longitudinal axis. In this arrangement the fuelair mixture (2025) being delivered into the cylindrical fuel chamber(3005) passes out of the cylindrical fuel chamber (3005) through each ofthe plurality of base wall fuel passages (3095) flows across the gapprovided between the surfaces of the interface (3032) and enters each ofthe corresponding catalyst fuel passage (3085). Once inside the catalystfuel passages (3085) the fuel air mixture begins to react with thecatalyst coated sidewall surfaces (3090) and the fuel air mixture beginsthe catalyzed partial oxidation reaction used to convert the fuel airmixture into reformed fuel or syngas. According to an aspect of thepresent disclosure, thermal energy generated by the CPOX reaction takingplace inside the catalyst fuel passages (3085) is radiated onto thebottom surface of the reactor shield base wall (3115) for partialabsorption thereby. Additionally, thermal energy generated by the CPOXreaction taking place inside the catalyst fuel passages (3085) isradiated onto inside surfaces of the base wall fuel passages (3095) forpartial absorption thereby.

The fuel reactor body (3040) is formed from materials having arelatively high thermal conductivity as compared to the thermalconductivity of the ceramic material used to form the cylindricalcatalyzing body (3030). A preferred reactor body material has acoefficient of thermal conductivity greater than 100 W/m° K. Thus, inone non-limiting example embodiment the entire fuel reactor body (3040)is formed from a unitary piece of copper or a copper alloy, from aunitary piece of beryllium or a beryllium alloy, from an unitary pieceof aluminum or an aluminum alloy, of a unitary piece of brass or a brassalloy, of a unitary piece of tungsten or a tungsten alloy, wherein thealloys may include molybdenum, nickel, chromium, brass, tungsten, or thelike. In the present example, unitary means the entire fuel reactor body(3040) is formed from a single piece of metal, e.g. cast or machined. Inalternate embodiments the fuel reactor body (3040) can be formed from aplurality of cast or machined elements that assembled together, e.g.welding, brazing, or mechanically fastening in a manner that provides acontinuous thermally conductive path. In any case a desired material hasa coefficient of thermal conductivity that is at least greater than 100W/m° K with some embodiments using materials having a coefficient ofthermal conductivity in excess of 300 W/m° K. Additionally, the wallthicknesses and or thermal mass of the fuel reactor body (3040) issufficient to promote rapid thermal conduction from a high temperatureregion of the reactor body (3040) proximate to the interface (3032) to alow temperature region of the reactor body (3040), e.g. the regiondisposed outside the hot zone, and to minimize temperature gradientsbetween the interface (3032) and the elements of the reactor body thatare disposed outside the hot zone. An additional characteristic of thereactor body material is that it preferably has a service temperature atleast exceeding 200° C. and preferably up to 1000° C.

In the present non-limiting exemplary embodiment, the fuel reactor body(3040) is formed from aluminum, preferably the Aluminum 6061 alloy, witha coefficient of thermal conductivity of approximately 167 W/m° K.Aluminum and aluminum alloys are preferred because they spontaneouslyform a stable oxide layer that protects the bulk structure fromcorrosive oxidative damage and can be used without an additional appliedprotective coating. Additionally, the aluminum and aluminum alloys canbe anodized to prevent or reduce surface oxidation. In a preferredembodiment the entire fuel reactor body (3040) comprises a solid elementcomprising a single piece of aluminum 6061 alloy; however, the fuelreactor body (3040) may comprise an assembly formed by assembling aplurality of individual subassembly elements together using mechanicalfasteners, welding or brazing, or using interlocking mechanicalfeatures, or the like, without deviating from the present disclosure.

More specifically according to an important aspect of the presentdisclosure the relative thermal conductivity of each of the cylindricalcatalyzing body (3030), the annular enclosure wall (3060) and the fuelreactor body (3040) is selected to promote thermal conduction from theinterface (3032) to a heat dissipating flange (3100), disposed outsidethe hot zone, and to promote absorption of thermal radiation impingingon surfaces of the reactor shield base wall (2015). This is accomplishedby configuring the fuel reactor body (3040) as the most thermallyconductive element local to the interface (3032) and by configuring thefuel reactor body (3040) to extend outside the hot zone where it iseither actively cooled e.g. by moving air passing over the surfaces ofthe fuel reactor body or passively cooled, e.g. by simply exposingsurfaces to the fuel reactor body (3040) to ambient air. Thus, theconfiguration of the fuel reactor body (3040) establishes and maintainsa temperature gradient between the interface (3032) and external ambientair, outside the hot zone, by providing a thermally conductive pathbetween the interface (3032) and a cooler portion of the fuel reactorbody which are provided by exposing a portion of the fuel reactor bodyto ambient air. The resulting temperature gradient between the portionof the fuel reactor body exposed to ambient air and the portion of thereactor body proximate to interface (3032) tends to promotesubstantially continuous thermal energy conduction through the fuelreactor body (3040) from the interface (3032) to the portion of the fuelreactor body that is exposed to ambient air.

The fuel reactor body (3040) includes a heat dissipating flange (3100),e.g. a disk shaped flange radially extending from the annular perimeterwall (3010). The heat dissipating flange (3100) is supported above thedisk shaped outer top wall (2516) external to the outer enclosure andexposed to surrounding air. Preferably the heat dissipating flange(3100) is integrally formed with the annular perimeter wall (3010) butthe heat dissipating flange (3100) may comprise a separate elementattached to the annular perimeter wall (3010) by welding, soldering,mechanical fasteners, or other attaching means.

An annular seal plate (3105) is disposed between the disk shaped outertop wall (2516) and the heat dissipating flange (3100) to provide amechanical interface between a top surface of the disk shaped outer topwall (2516) and a bottom surface of the heat dissipating flange (3100).The annular seal plate (3105) includes a centered through hole sized toreceive the annular perimeter wall (3010) there through. An O-ring sealelement (3110), or the like, is disposed between the annular seal plate(3105) and the heat dissipating flange (3100), e.g. in an O-ring groove,and serves to gas seal a top portion of the cylindrical catalyzingcavity (3035). A second O-ring seal element (3115), or the like, may beprovided between a top surface of the disk shaped outer top wall (2516)and a bottom surface of the annular seal plate (3105).

Both the annular seal plate (3105) and the heat dissipating flange(3100) are attached to the disk shaped outer top wall (2516) byfasteners, or the like, in a manner that applies a downward forceagainst the fuel reactor body (3040) in order to seat the bottom surfaceof the reactor shield base wall (3015) against the top surface of thecylindrical catalyzing body (3030) at the interface (3032), or theraised surfaces (3033) formed thereon, and further in order to compressthe O-ring seal element (3110).

Referring now to FIG. 6, a schematic top section view of the fuelreactor body (3040) depicts the heat dissipating flange (3100) radiallyextending from the annular perimeter wall (3010). Fasteners (3120)extend through the dissipating flange (3100) and the annular seal plate(3105) to attach the heat dissipating flange (3100) and the annular sealplate (3105) to the disk shaped outer top wall (2516). The annularperimeter wall (3010) extends radially outside the annular enclosurewall (3060) such that the seal plate (3105) seals the cylindricalcatalyzing cavity (3035). An array (3125) of base wall fuel passages(3095) is depicted passing through the reactor shield base wall (3015).

Referring now to FIG. 3, the fuel reformer system (3000) may includeexternal cooling and temperature sensing elements readable by theelectronic controller (190). In one non-limiting example embodiment, anair moving element (3130), such as a rotary fan blade attached to arotary motor, operable by the electronic controller (190), is disposedto direct air flow over the heat dissipating flange (3100), therebyincreasing convective thermal energy transfer from the flange (3100) tothe surrounding ambient air. Additionally, a temperature sensing element(3135) in contact with a surface of the heat dissipating flange (3100),or one or more other surfaces of the fuel reactor body (3040) is usableto deliver a temperature signal to the electronic controller (190) overa communication path (3140). Operation of air moving element (3130) maybe constant or may be variably triggered by changes in the temperaturesignal emitted by the temperature sensing element (3135). In onenon-limiting operating mode the air moving element (3130) is activatedwhen the temperature sensing element (3135) reports a temperature thatis above a desired high temperature limit, e.g. above 50° C., and theair moving element (3130) is deactivated when the temperature sensingelement (3135) reports a temperature that is below a desired hightemperature limit, e.g. below 45° C.

Additionally, the temperature signal emitted by the temperature sensingelement (3135) is usable to control operation of the cold startcombustion chamber (2300) such as to stop fuel flow to the cold startcombustion chamber (2300) when the temperature of the heat dissipatingflange (3100) reaches a desired steady state temperature range.

In an example operating mode, the electronic controller (190) receivestemperature signals from the temperature sensing element (3135) overcommunication pathway (3140) and determines an instantaneous flangetemperature based thereon. The electronic controller (190) thendetermines whether the flange temperature is within one or more desiredtemperature ranges and if not carries out various commands such as tooperate or stop operating the air moving element (3130) and or to startor stop fuel flow to the cold start combustion chamber (2300) or tocease fuel delivery to the fuel reformer system (3000) by commanding thefuel delivery module (197) to close a gas flow actuator valve, or thelike, when the instantaneous temperature indicated by the temperaturesensing element (3135) exceeds a safe operating limit. In onenon-limiting operating mode the electronic controller (190) isconfigured to activate the air moving element (3130) when thetemperature of the heat dissipating flange (3100) exceeds 50° C. Inother example embodiments the air moving element (3130) may havemultiple operating modes usable to move more or less air depending onneed based on different temperature thresholds.

8.6 The Interface Configuration

Referring now to FIG. 4 an exploded side section view of the interface(3032) between corresponding pairs of base wall fuel passages (3095) andcatalyst fuel passages (3085), shows that each corresponding pair ofreactor shield base wall fuel passages (3095) and catalyst fuel passages(3085) is aligned along a common longitudinal axis. Thus, eachcorresponding pair of base wall fuel passages and catalyst fuel passagesprovides a vertical flow path through which the fuel air mixture passesfrom the cylindrical fuel chamber (3005) to the fuel inlet manifold(3055). As noted above a gap may be provided between the mating surfaceof the interface (3032) to expose surfaces of the reactor shield basewall (3015) to thermal radiation being emitted by the CPOX reaction butthe gap is not shown in FIG. 4 to simplify the disclosure. As indicatedby the reference number (3090) a catalyst layer is formed on thesidewall of each catalyst fuel passage (3090). As is further shown inFIG. 4, a pointer referring to FIG. 4A indicates that FIG. 4A depicts aschematic view of the interface (3032) as viewed from inside a catalystfuel passage (3085) looking toward its fuel input end. In the presentnon-limiting example embodiment, the diameter (D) of each of thecircular base wall fuel passages (3095) is 1.3 mm and the thickness ofthe reactor shield base wall is 13 mm such that each fuel passage (3095)is 13 mm long. In a preferred embodiment the ratio of fuel passagelongitudinal length to its diameter is at least 5, preferably 10 and upto 20. The side wall dimension of each of the square catalyst fuelpassages (3085) is 1.3 mm and the thickness of the cylindricalcatalyzing body (3030) is about 25.4 mm such that each catalyst fuelpassage (3085) is 25.4 mm long. In a preferred embodiment the ratio ofcatalyzing passage longitudinal length to its square side dimension isat least 10, preferably 15-25 and up to 40.

The cylindrical catalyzing body (3030) has a circular cross-section andan array of catalyzing fuel passages (3085) is formed within thecircular cross-section over a circular region having a diameter of 25.4mm (1.0 in.) Each of the catalyzing fuel passages of the array has asquare cross-section and extends completely through the cylindricalcatalyzing body (3030). In the present non-limiting exemplary embodimenteach square catalyzing fuel passage has a side dimension of 1.3 mm and alength of 25.4 mm. Alternately, the catalyzing body (3030) and the arrayof fuel passages can have other non-circular cross-sections withoutdeviating from the present disclosure.

The reactor shield base wall (3015) is formed with an array of circularbase wall fuel passages (3095) formed within a 25.4 mm (1.0 in.)diameter circular array region opposed to the circular array region ofthe cylindrical catalyzing body (3030). In the present non-limitingexemplary embodiment each circular base wall fuel passage (3095) has adiameter of 1.3 mm and a length of 13.0 mm. Alternately, the reactorshield base wall (3015) and the array region formed thereon can haveother non-circular cross-sections without deviating from the presentdisclosure. As described above each circular base wall fuel passage(3095) in the array of base wall fuel passages is coaxial with one ofthe square catalyst fuel passages (3088) in the array of catalyst fuelpassages such that a central longitudinal axis of each base wall fuelpassage (3095) is coaxial with a central longitudinal axis of acorresponding catalyst fuel passage (3085).

Solid material of the reactor shield base wall (3015) surrounds eachcircular base wall fuel passage and solid material of the cylindricalcatalyzing body (3030) surrounds each square catalyst fuel passage. In anon-limiting exemplary array pattern, all the passages are arranged in aplurality of parallel linear arrays. Each linear array is offset from anadjacent linear array by the same pitch dimension of 1.2 times thecircular passage diameter. In the present example the pitch dimension is1.56 mm. Based on this non-limiting exemplary array disposed over a 25.4mm diameter circle, the total number or circular passages (3095) in thecircular array area is approximately 208.

The combined area of the 208 passages each having a 1.3 mm diameter is276 mm². The total area of the 25.4 mm diameter array area is 507 mm².Thus, the area of solid material in the circular array area isapproximately 231 mm² such that the bottom surface of the reactor shieldbase wall (3015) provides about 231 mm² of surface area facing theinterface (3032) that is available to absorb radiant thermal energyimpinging thereon. In the present example embodiment, the ratio of solidsurface area to hole diameter area is 0.84. As a percentage of the totalarea of the circular array about 54% of the total area is circularpassage area and about 46% of the total area is solid material area. Aswill be recognized by those skilled in the art the ratio of surface areato hole diameter area can be increased by decreasing the diameter of thecircular base wall fuel passages. Since the surface area at theinterface (3032) is impinged by radiant thermal energy emitted by theCPOX reaction, increasing the solid surface area, without a change intemperature, increases thermal energy absorption into the reactor shieldbase wall (3015). In a preferred embodiment the ratio of solid surfacearea to hole diameter area ranges between 0.75 to 0.9.

As noted above radiant thermal energy emitted by the CPOX reaction alsoenters the circular base wall fuel passages (3095) and at least aportion of the radiant thermal energy impinges onto inside surfacesthereof. While the incident angle of radiant thermal energy impinging onthe inside surfaces of circular base wall fuel passages (3095) is nearlygrazing, the passages are long compared to the passage diameter andreflected energy, even when reflected at near grazing incidence isscattered and ultimately impinges onto and reflects from the insidesurfaces over many reflection cycles as it traverses a fuel passage(3095). The total surface area of inside surfaces of all 208 circularpassages is about 11043 mm².

Referring now to FIG. 4A the figure depicts the interface (3032) of asingle circular fuel passage (3095) and a single square catalyst fuelpassage (3085) as viewed from the fuel inlet manifold (3055). As furthershown, according to the present disclosure, each base wall passage(3095) has a circular cross-section having a diameter (D) along itsentire longitudinal length and each catalyst fuel passage (3085) has asquare cross-section having a side dimension (S) along its entirelongitudinal length. In the non-limiting exemplary embodiment of FIG.4A, the diameter (D) and the side length (S) are equal and an area (B),shown filled with vertical lines, is an exposed surface area of thebottom surface of the reactor shield base wall (3015). The surface area(B) is located at the interface (3032) proximate to the input end ofeach catalyst fuel passage (3085) and is specifically provided to absorbthermal radiation being radiated from the catalyzing surface (3090).Additionally, when a gap between the opposing surfaces of the interface(3032) is provided, thermal radiation enters the gap in part byreflecting from surface area (B).

Equation (1) below provides the area of surface area (B):

A _(s) −A _(c) =S ²-π(D/2)²  EQU: 1

where A_(s) is the area of a square (3085) having side length (S)

A_(c) is the area of a circle (3095) having diameter (D).

In the case where S=D the surface area AB of the surface area (B) is:

(A _(B))=S ²(1—π/4)=0.2146S ²  EQU: 2

In other words, the area of surface (B) is about 21% of the area of thesquare (3085). As will be recognized, the area AB can be increased toincrease exposure of the surface (B) to thermal radiation beinggenerated inside the catalyzing fuel passages e.g. by increasing thesquare side dimension from (S) to (S1), or by decreasing the diameter(D) of the circular passages (3095). When the side dimension of acatalyst fuel passage is increased from (S) to (S1) the area SB can beincreased to 50% of the area of the square of dimension (S1) when theratio S1/D is equal to about 1.253.

The surface area (B) is directly exposed to the CPOX reaction takingplace inside the square catalyst fuel passages (3085) and is in the bestposition to absorb thermal energy radiating out of the catalyst fuelpassages. In a non-limiting exemplary embodiment of the presentdisclosure even when there is no gap at the interface (3032) the surface(B) as well as the inside surfaces of the base wall fuel passages (3095)provide sufficient surface area of the cooler reactor shield base wall(3015) to absorb sufficient radiant thermal energy emitted by the CPOXreaction to prevent catalyst layer burn through. However, as will berecognized by those skilled in the art, when the gap is provided,additional radiant thermal energy enters the gap and may impinge ontoand be reflected from the cooler solid material surface areas of thereactor shield base wall (3015) over many cycles to absorb additionalthermal energy emitted by the CPOX reaction.

8.7 Thermal Energy Transfer

Without wishing to be bound by theory, Applicants believe that theexothermic catalyzed partial oxidation reaction is initiated immediatelyupon contacting the catalyst layer (3090) proximate to the interface(3032) when the fuel air mixture (2025, 3025) is heated to a suitablereaction temperature. Additionally, Applicants believe that theexothermic catalyzed partial oxidation reaction reaches its maximumtemperature proximate to the interface (3032), with the maximumtemperature approximately between 900 and 1000° C. In response to therapid heating proximate to the interface (3032), the temperature of thefuel air mixture entering the catalyst fuel passages (3085) and of thecatalyst layers (3090) rapidly increases as thermal energy is absorbedby the fuel air mixture as well as by the catalyst layers (3090). Inresponse to the temperature increase, the fuel air mixture rapidlyexpands in volume to fill the catalyst fuel passages (3085) and exitfrom catalyst fuel passages to fill the cylindrical catalyzing cavity(3035) and the fuel inlet manifold (3055). During the gas expansion moreof the fuel air mixture comes into contact with the catalyzing layer(3090) distal from the interface (3032) to participate in the exothermiccatalyzed partial oxidation reaction, thereby further heating andexpanding the fuel/air mixture. Thus, most of the thermal energygenerated by the catalyzed partial oxidation reaction is absorbed by thefuel/air mixture and carried out of the catalyst fuel passage to thefuel inlet manifold (2055). In an example operating mode, the volume offuel/air mixture delivered into the CPOX reactor is believed to generateabout 300 watts during the CPOX reaction.

A portion of the thermal energy generated by the catalyzed partialoxidation reaction is absorbed by the catalyzing layer (3090). In thepresent example the catalyst layer is metallic (e.g. Rh), with acoefficient of thermal conductivity of about 150 W/m° K. Thus, thermalenergy absorbed by the catalyzing layer (3090) is thermally conductedthrough the catalyzing layer thickness to reach the ceramic catalyzingbody (3030) and is further conducted along the longitudinal length ofthe catalyzing layer (3090. However, since the catalyst body (3030) is aceramic material with a coefficient of thermal conductivity of about 45W/m° K, the heat flux density (W/m²) entering the ceramic material islow resulting in thermal energy absorbed by the catalyzing layer beingreemitted into the catalyzing fuel passages instead of being thermallyconducted into the ceramic material. However this result is desirablesince the low heat flux density along the radial axis of the ceramiccatalyzing body prevents thermal energy from being conducted radiallyaway from the catalyzing fuel passages to the extent that thermal energyis either a) transferred to the fuel air mixture inside the fuelpassages, orb) radiated out of the ends of the fuel passages either tothe fuel inlet manifold or onto the surface area (B) described above, orc) radiated onto other exposed solid material surfaces of the reactorshield base wall, e.g. by entering the gap provided at the interface, ord) radiated into the circular base wall fuel passages to either betransferred to the incoming gas air mixture by convective heat transfer,or e) radiated onto inside surfaces of the base wall fuel passages(3095) to be absorbed thereby.

Thus, thermal energy absorbed by the catalyzing layer is not readilydissipated to the ceramic catalyzing body (3030). Instead the thermalenergy is reemitted into the catalyzing fuel passage to further heat thefuel air mixture. Additionally, thermal energy emitted or reflected bythe catalyzing layer impinges onto other surfaces of the catalyzinglayer and is partially absorbed and partially reflected thereby.However, without at least one outlet for thermal radiation to exit thecatalyst fuel passage the energy absorption rate of the catalyzing layer(3090) may exceed the energy reemission rate thereby causing thetemperature of the catalyzing layer to continue to increase until itreaches a temperature that causes the catalyzing layer to burn offcausing permanent damage to catalyzing fuel passages.

As described above Applicants believe that the total power generated bythe CPOX reaction is 300 W. Using the Stefan Boltzmann equation listedbelow as Equation 3 the total power that can be absorbed by thecollective surface area (B) shown in FIG. 4A, i.e. based on 208 basewall passages (3095) can be estimated given the surface area andtemperature.

P=eσAS _(f)(T _(c) ⁴ −T _(b) ⁴)  EQU. 3

where: P=net absorbed power (watts); e=surface emissivity; σ=5.6703×10⁻⁸(W/m²K⁴) the Stefan Boltzmann constant; A=area onto which radiation isradiated (m²); Sf—a form factor related to the incidence angle at whichthe radiation impinges on the surface area A; T_(c)=temperature ofradiation source (° K); and T_(b)=temperature of the surface area A (°K).

Of particular importance is the fact that when Tc and Tb are equal.Equation 3 shows that the net radiated power absorbed by the reactorshield base wall (3015) is zero. Thus, without cooler surface areasprovided by the reactor shield base wall (3015) the surface temperaturesinside the catalyst fuel passages can continue to increase until thecatalyst layer overheats and burns through.

In a non-limiting example embodiment wherein, each square catalyst fuelpassage (3085) has a side dimension (S) equal to 1.3 mm (0.0013 m) andeach circular base wall passage (3095) has a diameter of 1.3 mm, thecollective area of all the surface areas (B), denoted ABt for an arrayof 208 passages is 7.38×10-5 m². Assuming that the CPOX reactiontemperature is 1000° C. (1273° K) and the temperature of each surfacearea AB is 100° C. (373° K) and using the simplified case where theemissivity e=1.0, Equation 3 predicts that the combined surface area ABtcan absorb about 11 W or about 3.6% of the power generated by the CPOXreaction.

If a gap is provided at the interface (3032) such that the entire solidsurface area of the bottom surface of the reactor shield base wall(3015), denoted AS is potentially available to absorb thermal energy,the available solid material surface area AS is 2.31×10⁻⁴ m² andEquation 3 predicts that the area AS can absorb about 34 W or about11.3% of the power generated by the CPOX reaction.

If in addition the surface area of the inside surfaces of all 208circular fuel passages (3095) is potentially available to absorb thermalenergy, the available surface area of all the circular fuel passages,denoted AP is 1.1043×10⁻² m² and Equation 3 predicts that the surfacearea AP can absorb about 1632 W or about 211% of the power generated bythe CPOX reaction.

As a practical matter, the above listed thermal energy absorption powervalues are calculated using a form factor Sf=1 which is the case whenthe thermal radiation impinges the surface at normal incidence. Whilethis may be the case for the surface area ABt, a value of Sf=1 is notrealistic for the surfaces areas AS and AP. Additionally as a practicalmatter the surface emissivity (e) of a heavily oxidized aluminum surfaceis not 1.0 but instead is about 0.25 or less. Accordingly, the energyabsorption values are more realistically represented when Equation 3 isused with surface emissivity e=0.25 for all three surfaces areas ABt,AS, and AP and with the form factor Sf=1 for the surface area ABt, andSf=0.1 for the surface areas AS and AP. In this case, Equation 3predicts that the surface area ABt potentially absorbs about 2.75 W, thesurface area AS potentially absorbs about 0.85 W and the surface area APpotentially absorbs about 44.6 W. Thus, the reactor shield base wall(3015) when maintained at about 100° C. potentially absorbs about 16% ofthe total power emitted by the CPOX reaction.

Those skilled in the art will recognize that additional thermal energycan absorbed by increasing the available surface area or by lowering thetemperature of the reactor shield base wall (3015). As noted aboveaccording to the present disclosure the surface temperature of the heatdissipating flange (3100) is preferably maintained in a range of 50-100°C. which due to the high thermal conductivity of the fuel reactor body(3040) likely maintains the temperature of the entire reactor shieldbody (3040) at nearly the same temperature but provides a thermalgradient between the fuel reactor base wall (3015) and the heatdissipating flange (3100). As noted above this allows thermal energy tobe absorbed from the CPOX reaction and prevents the unprocessed fuelpassing through the fuel reactor body (3040) from reaching its autoignition temperature of 295 to 580° C., depending on which fuels are inuse.

Thus, maintaining the reactor shield base wall (3015) described above ata temperature of 100° C. during operation and providing a small gap,e.g. about 1 mm at the interface (3032) has the potential of absorbingabout 43 W of thermal energy or about 14% of the total energy beingradiated by the CPOX reaction at a temperature of 1000° C. However,those skilled in the art will recognize that increasing the shapefactor, increasing the surface area and decreasing the temperature ofthe fuel reactor body (3040) can remove additional thermal energy fromeach of the catalyst fuel passage (3085).

8.8 Operating Mode

8.8.1 Cold Start

Referring to FIGS. 1-3, from a cold start, the fuel input module (197)is operated by the electronic controller (190) to deliver a fuel airmixture into the cold start combustion chamber (2300) through a fuelinput inlet (2304) and to ignite the fuel air mixture inside the coldstart combustion chamber (2300) with an electric igniter (2306) operableby the electronic controller (190). At the same time or shortlythereafter the fuel input module (197) also operates to deliver fuel/airmixture into the fuel reformer module (3020) through the fuel inputconduit (2045) and the fuel air mixture passes through the fuel reformermodule (3020) to the fuel input manifold (2055). Preferably the initialflow rate of the fuel air mixture being delivered through the fuelreformer module is very low and is intended to merely fill the SOFCsystem with a nearly stationary volume of fuel air mixture.

The ignited fuel inside the cold start combustion chamber (2300) heatswalls of the cold start combustion chamber (2300) but the top end wall(2017) is configured to absorb more thermal energy than the other wallsof the cold start combustion chamber. As the temperature of the top endwall (2017) increases, thermal energy is thermally conducted from thetop end wall (2017) to other regions of the hot zone enclosure walls(115). Additionally, the top end wall (2017) and other walls of the hotzone enclosure (115) begin to emit thermal radiation into the fuel inletmodule (2055) which is absorbed by the fuel air mixture containedtherein, increasing its temperature. Exhaust gas generated by combustingthe fuel air mixture inside the cold start combustion chamber (2300)exits from the cold start combustion chamber (2300) through cold startexit ports (2302) and flows through the air gap (2155) to a system exitport (2165). As the hot exhaust gas flows through the air gap (2010) itradiates thermal energy to outside surfaces of the longitudinalcylindrical side wall (2015) which increase in temperature.

The top end wall (2017) is attached to the longitudinal cylindrical sidewall (2015) which is further attached to disk shaped bottom tube supportwall (2084) and disk shaped separator wall (2214). Each of the top endwall (2017), the longitudinal cylindrical side wall (2015), the diskshaped bottom tube support wall (2084) and the disk shaped separatorwall (2114), collectively form the hot zone enclosure walls (115). Asnoted above, each of the hot zone enclosure walls is fabricated from oneor more of copper, molybdenum, aluminum copper, copper nickel alloys, ora combination thereof such that the entire hot zone enclosure wallstructure (115) forms a continuous thermally conductive path having acoefficient of thermal conductivity between about 100 and 300 W/m° K,and preferably above 200 W/m° K. Additionally, where surfaces of any ofthe hot zone enclosure walls are exposed to an oxygen rich environmentthe wall surfaces are preferably nickel coated to prevent oxidation.

In the case of the three disk-shaped walls, (2017, 2084, and 2214), eachof these walls is configured to provide a thermal mass that is capableof absorbing and redistributing thermal energy to other regions of thehot zone enclosure walls by thermal conduction and by reemitting theabsorbed thermal energy to cooler areas surrounding each disk-shapedwall such as into the fuel inlet manifold (2055), the cathode chamber(2010), the combustion chamber (2135) and the recuperator chamber(2210). Thus, as the top end wall (2017) is heated by combustion insidecold start combustion chamber (2300) thermal energy is absorbed by thetop end wall and rapidly conducted to all regions of the hot zoneenclosure walls (2017), 2015, 2084, and 2214) until the entire hot zoneenclosure wall assembly reaches an equilibrium temperature. Moreover, asthermal energy is absorbed or emitted by the hot zone enclosure wallsits equilibrium temperature varies substantially uniformly across allregions of the hot zone enclosure walls due to its high thermalconductivity.

Thus, during the startup period at least a portion of the thermal energygenerated by combustion of fuel in the cold start combustion chamber(2300) is absorbed by top end wall (2017). A further portion is absorbedby the longitudinal cylindrical sidewall (2015) as the hot exhaust gasflows through the air gap (2155) to the system exit port (2165). As thetemperature of the top end wall (2017) increases, the top end wall(2017) begins to reemit thermal energy into the cooler fuel inletmanifold (2055) which serves to increase the temperature of whateverfuel air mixture is contained therein and or flowing there through.

Eventually, the temperature of the fuel air mixture inside the fuelinlet manifold (2055) reaches a reaction temperature suitable forinitiating a CPOX reaction. The initial CPOX reaction occurs when thefuel air mixture having been heated to the reaction temperature makescontact with the catalyst layers (3090) proximate to the catalyzing bodyinput or top surface located at the interface (3032) where thecatalyzing body interfaces with the back end or bottom surface of thefuel reformer module (3020). Once the CPOX reaction is initiated at theoutput ends of some or all of the catalyst fuel passages (3085) thetemperature inside each catalyst fuel passage (3085) rapidly increasesalong its longitudinal length spreading the CPOX reaction to theinterface (3032) and the CPOX reaction becomes self-sustaining.

Once a self-sustaining CPOX reaction is achieved, the fuel input module(197) is operated to discontinue the flow of fuel air mixture to thecold start combustion chamber (2300) and to adjust the input rate of thefuel air mixture being delivered though the fuel reformer module (3020)as required to maintain the self-sustaining CPOX reaction and generateelectrical power. However, combustion inside the cold start combustionchamber (2300) may be continued until full power DC power output is alsoself-sustaining. The electronic controller (190) can become aware of theself-sustaining CPOX reaction by various sensors including temperaturesensors provided on a wall of the hot zone enclosure, by the temperaturesensor (3135) provided on the heat dissipating flange (3100), by atemperature sensor provided proximate to the system exhaust port (2165),by detecting a DC power signal at the DC power output module (140) andby various other sensing means.

To heat the cathode gas, the electronic controller (190) operates theair input module (198) to deliver a flow of air/cathode gas, into theair input port (2205). While this step can be taken simultaneously withigniting the cold start chamber or even before igniting the cold startchamber, it can also be delayed until a self-sustaining CPOX reaction isachieved. Preferably the initial flow rate of the incoming air beingdelivered through the recuperator chamber (2210) is very low and isintended to merely fill the SOFC system with a nearly stationary volumeof air.

The flow of incoming air exits the cathode feed tube (2145) through therecuperator input port (2235), passes through the recuperator chamber(2210) to the recuperator output port (2235) and the exits the cathodefeed tube (2145) to the cathode chamber (2010) through the plurality ofair exit ports (2240). After reacting with the solid oxide cathodeelectrode formed on outside surfaces of each tubular fuel cell (2080)the air/cathode gas, exits the combustion chamber (2135), passingthrough the cathode chamber exit ports (2245) to the combustion chamber(2135) where it mixes with spent fuel air mixture and for combustion.Thereafter the combustion byproducts exit the combustion chamber throughcombustor exit ports (2150) to the air gap (2155) and out of the systemthrough the system exit port (2165).

The main air heating element is the disk-shaped separator wall (2214)provided inside the recuperator chamber (2210). As described above, thedisk-shaped separator wall (2214) is part of the hot zone enclosure andtherefore begins to increase in temperature during the start-up phasealmost concurrently with increases in temperature of the disk-shape topend wall (2017) that forms the base wall of the cold start combustionchamber (2300). Additionally, the disk-shaped separator wall (2214) isthermally conductively coupled to the disk-shaped bottom tube supportwall (2084) and both walls are heated by combusting the mixture of spentfuel and spent air inside the combustion chamber (2135). Thus, at aboutthe same time that the disk-shape top end wall (2017) begins to radiateenough thermal energy into the fuel input manifold (2055) to raise fueltemperature, the disk-shaped separator wall (2214) begins to radiateenough thermal energy into the recuperator chamber (2210) to raise thetemperature of the incoming air. At the same time the hot zone enclosurewalls are radiating thermal energy into the cathode chamber (2010) whichserves to heat the air contained therein and to heat the walls of thetube shaped fuel cells of the fuel cell stack (2005). Once the CPOXreaction becomes self-sustaining the flow rate of both the incoming airand the fuel air mixture may be adjusted as required to maintain theself-sustaining CPOX reaction and to generate electrical power atdesired power output amplitude.

8.8.2 Initiating an SOFC Reaction

As described above, the fuel air mixture and the incoming air/cathodegas are heated by the hot zone enclosure walls which are heated bycombustion taking place inside the cold start combustion chamber (2300).Eventually a self-sustaining CPOX reaction is initiated inside thecatalyst fuel passages (3085) which heats the fuel air mixture to ahigher temperature and the fuel is reformed into a syngas which iscapable of reacting with the solid oxide anode electrodes formed on theinside surfaces of each of the tubular fuel cells (2080). The highertemperature syngas also radiates thermal energy onto the anode electrodeelectrodes as it passes through the tubular fuel cells (2080). As thetemperature of the anode electrode increases the cathode electrode isheated by thermal energy being radiated into the cathode chamber (2010)by the longitudinal cylindrical sidewall (2015) and heated air/cathodegas entering the cathode chamber (2010) from the recuperator chamber(2210).

Eventually the anode and cathode electrodes, the syngas and theair/cathode gas inside the cathode chamber reach a reaction temperaturewhere DC power begins to be generated and output to the DC powerterminals. Eventually the gas temperature inside the combustion chamber(2135) reaches a combustion temperature and the thermal energy generatedby the combustion occurring inside the combustion chamber increases theincoming air temperature to a steady state operating temperature. In onenon-limiting example operating mode, the syngas, the incoming air andthe tubular fuel cells (2080) have a steady state operating temperatureof between 350 and 1200° C. with a preferred operating temperature rangeof 800-1000° C. Meanwhile the hot zone enclosure walls (115) constantlyredistribute thermal energy by thermal conduction such that the hot zoneenclosure wall temperature increases and decreases substantiallyuniformly over all regions thereof until a steady state operatingtemperature is reached and then maintained.

8.8.3 Fuel Reformer Operating Mode

Referring now to FIGS. 3-4A, as described above, the fuel reformermodule (3020) is at least partially thermally isolated from the coldstart combustion chamber (2300) and the hot zone enclosure walls inorder to prevent the fuel air mixture inside the fuel chamber (3005)from reaching its auto ignition temperature prior to entering thecylindrical catalyzing body (3030). More specifically depending on thefuel being used the fuel auto ignition temperature range isapproximately 295 to 580° C. By comparison the operating temperaturerange of the SOFC system, again depending on fuel and electrode layermaterials, is 350 to 1200° C. Additionally, as pointed out above theCPOX reaction temperature range is estimated to be 900 to 1000° C.

During a cold start, the fuel air mixture (3020) enters the cylindricalfuel chamber (3005) and passes through the reactor shield base wall(3015) and then through the cylindrical catalyzing body (3032) to thefuel input manifold (3055). The fuel air mixture then flows through thetubular fuel cells and eventually out of the system. As described above,the present disclosure manages thermal energy generated by combustioninside the cold start combustion chamber (2300) in a manner thatfacilitates a greater transfer of thermal energy to the disk shaped topend wall (2017) of the hot zone enclosure than is transferred to theother cold start combustion chamber walls (2510 and 2511) and (2513).This is managed by configuring the disk shaped top end wall (2017) witha greater thermal mass than the combined thermal mass of the other walls(2510 and 2513).

More specifically, thermal energy transfer (Q) is governed by Equation4:

Q=Q=C _(th) ΔTQ  EQU. 4

where: Q=thermal energy transfer (J); C_(th)=thermal mass of wall (J/°C.); and ΔT=temperature difference between the hot gas and the wall.

In the present example. ΔT is approximately the same for each wall;however, the thermal mass of each wall is different. The thermal massC_(th) is defined as the product of wall material mass (m) in units of(g) and the specific heat capacity (μ) in units of (J/g° C.) of thematerial, where mass (m) is the product of wall material volume V, inunits of (cm³), and the material density (ρ), in units of (g/cm³).

C _(th) =ρVμ  EQU. 5

where: ρ=material density (g/cm³); V=material volume (cm³); andμ=material specific heat capacity of the material (J/g° C.).

In a non-limiting example embodiment, the disk shaped top end wall(2017) of the hot zone enclosure comprises mostly copper and the otherwalls (2510), (2511) and (2513), of the intermediate enclosuresurrounding the cold start combustion chamber (2300) and furthersurrounding the hot zone enclosure each comprises mostly Hastelloy. Forcopper, the specific heat capacity (μ) is 0.385 J/g° C. For Hastelloy,which is a Cobalt-Nickel-Chromium-Tungsten alloy that combines excellenthigh temperature strength with very good resistance to oxidizingenvironments up to 2000° F. (1095° C.), the specific heat capacity GO is0.450 J/g° C. For copper, the density (p) is 8.96 g/cm³ and forHastelloy the density (p) is 8.22 g/cm³. Ensuring that the top end wall(2017) absorbs more thermal energy that the other walls, proximate tothe cold start chamber (2300), combined is accomplished when (Q_(t)) ofthe disk shaped top end wall (2017) is greater that (Q_(o)) of all theother walls combined which when expressed in terms of Equation 4 whenthe term AT is the same for each wall simplifies to:

C _(th) t>C _(th) o or (ρ_(c) Vtμ _(c))>(ρ_(h) Voμ _(h))

where: C_(th)t=thermal mass of the top end wall; C_(th)o=thermal mass ofthe other walls combined; Vt=volume of the top end wall; Vo=volume ofthe other walls combined; ρ_(c)=density of copper and ρ_(h)=density ofHastelloy; and μ_(c)=specific heat of copper and μ_(h)=specific heatHastelloy;

with the result of the present example that:

V _(t)>1.07V _(o)

In other words, the thermal mass of the top disk shaped top end wall(2017) exceeds the thermal mass of other cold start combustion chamberwalls (2510 and 2513) when the volume (Vt) of the disk shaped top endwall (2017) exceeds 1.07 times the combined volume (Vo) of the otherwalls (2510 and 2513). Thus, according to the present disclosure, thethermal mass of the top disk shaped top end wall (2017) exceeds thethermal mass of the intermediate enclosure walls (2510 and 2513) andpreferably by 100% or more. More practically only the walls actuallysurrounding cold start chamber (2300) are taken into account tocalculate (Vo) above. In the above example, (Vo) includes the entirevolume of wall (2513) and only that portion of the wall (2510) thatactually encloses the cold start chamber (2300). Using this model, thethermal mass of the wall (2513) and the portion of the wall (2510) thatsurrounds the cold start chamber, is exceeded by 100% when the volume ofthe disk shaped top end wall (2017) (Vt), is 2.14 times the volume (Vo).

As a result, more thermal energy is absorbed by the top end wall (2017)than is absorbed by all the other cold start combustion chamber wallscombined. A primary advantage of this embodiment is absorbing themajority of thermal energy generated by the fuel air mixture beingcombusted inside the cold start combustion chamber (2300) into the topend wall (2017). Since the top end wall and the other hot zone enclosurewalls are more thermally conductive than the walls (2510 and 2513)thermal energy absorbed by the top end wall is rapidly conducted by thethermally conductive path formed by hot zone enclosure walls. This isfurther facilitated by forming the intermediate enclosure walls (2510,2511, and 2513) and the annular enclosure wall (7060) from Hastelloy oranother high nickel content metal having a coefficient of thermalconductivity of less than about 25.0 W/m° K which causes a much slowerconductive heat flow rate away from the hot zone enclosure walls thanthrough the hot zone enclosure walls.

During the cold start process combustion energy from the cold startchamber is primarily absorbed by the top end wall (2017) and reemittedinto the fuel inlet manifold (2055) to sufficiently heat the fuel airmixture contained therein to a temperature that is high enough toinitiate the CPOX reaction at the output end (3034) of the catalyst fuelpassages (3085). A secondary advantage of this embodiment is that themajority of thermal energy generated by the fuel air mixture beingcombusted inside the cold start combustion chamber (2300) is divertedaway from the fuel reformer module (3020) by instead providing a higherconductive heat flow rate from the disk shaped top end wall (2017) tothe other hot zone enclosure walls (2015 and 2511) as well as to thedisk shaped separator wall (2214) and the disk-shaped bottom tubesupport wall (2084).

Once the CPOX reaction is initiated and self-sustaining the fuel reactorbody (3040) provides a thermally conductive path and sufficient thermalmass to rapidly conduct thermal energy from the reactor shield base wall(3015) to the heat dissipating flange (3100). In particular since theinterface (3032) is proximate to the CPOX reaction which has atemperature of 900-1000° C., thermal energy reaches the reactor shieldbase wall (3015) in varying amounts by radiation, thermal conduction,and convection and is absorbed by the exposed surface (B) and theremaining solid material of the bottom surface of the reactor shieldbase wall (3015), as well as internal surfaces of the circular base wallfuel passages (3095) shown in FIGS. 4 and 4A. As a result, the initialCPOX reaction proximate to the interface (3032) is effectively quenchedto prevent auto ignition of the incoming fuel air mixture. The combinedsurface area (B) denoted ABt potentially absorbs about 1% of the totalthermal radiation emitted from all the catalyst fuel passage (3085) andthe solid surface area of the reactor shield base wall at the interface,denoted AS above, potentially absorbs about 0.2% of the total thermalradiation emitted from all the catalyst fuel passage (3085) and internalsurfaces of the base wall fuel passages (3095) potentially absorb about13.6% for a combined total of about 15%.

According to the present disclosure the thermal mass of the reactorshield base wall (3015), i.e. its material volume, (see equation 5above), is formed large enough to provide sufficient energy transferfrom the catalyst fuel passages (3085) to prevent over heating thereinwhen the reactor shield base wall can be maintained at or below 100° C.Additionally according to the disclosure the thermal mass of the fuelreactor body (3040), i.e. its material volume, is formed large enough toprovide sufficient energy transfer by thermal conduction from thereactor shield base wall (3015) to the heat dissipating flange (3100) toallow the entire fuel reactor body (3040) to be maintained nearly atuniform temperature with a small thermal gradient maintained between thehigher temperature reactor shield base wall and the heat dissipatingflange (3100). Additionally according to the present disclosure thesurface area of the heat dissipating flange (3100) is sufficiently largethat thermal energy is dissipated therefrom at a rate equal to the rateof thermal energy being absorbed by the reactor shield base wall (3015),which as noted above is about 44 W. Additionally according to thepresent disclosure the fuel reactor body (3040) is configured todissipate sufficient thermal therefrom to prevent the fuel air mixturepassing through the cylindrical fuel chamber (3005) from exceeding anauto ignition temperature thereof. More specifically the heatdissipating flange (3100) is configured to dissipate enough thermalenergy to the surrounding air to maintain the temperature of the fuelreactor body (3040) below about 295° C., equal to the lowest autoignition temperature of expected fuel air mixtures, and preferably tomaintain the temperature of the entire fuel reactor body (3040) betweenabout 100 and 250° C. during all operating modes. Also according to thepresent intention, temperature of the heat dissipating flange (3100) ismonitored during all operating phases and if the temperature of the heatdissipating flange exceeds a desired high temperature limit, in a rangeof 100 to 250° C., the input fuel air mixture may be stopped by operableelements of the fuel input module (197) to prevent fuel from enteringthe reformer (167) until further operation or the air moving element(3130) reduces the temperature the heat dissipating flange (3100) to asafe operating temperature.

8.9 Alternative Fuel Reformer and Outer Enclosure Embodiment

Referring now to FIGS. 2-4 and 7, an exemplary, non-limiting,alternative embodiment of an SOFC system (7000) includes an alternateembodiment of a fuel reformer module (7020) and related elements. TheSOFC system (7000) has substantially identical construction and similaroperating modes as compared with the systems (2000 and 3000) shown inFIGS. 2-4, both described above, except that additional features anddifferent operating modes of the system (7000) are outlined below. Inorder to clarify the similarity and differences between the systems theSOFC system embodiments (2000, 3000, and 7000) below, like referencesnumbers are used when the referenced item has substantially the samestructure in each of the systems (2000, 3000, and 7000).

Referring to FIG. 7 an alternate fuel reformer module (7020) includes afuel reactor body (7040) comprising an annular perimeter wall (7010)attached to or integrally formed with a reactor shield base wall (7015).The fuel reactor body (7040) is formed to provide a cylindrical fuelchamber (7005) bounded by the annular perimeter wall (7010), the reactorshield base wall (7015) and by a disk shaped outer enclosure top endflange (7102). A fuel inlet conduit (7045) is disposed to pass throughthe disk shaped outer enclosure top end flange (7102) to fuel chamber(7005).

The fuel reformer module (7020) further includes a cylindricalcatalyzing body (3030), described above. Each of the fuel reactor body(7040) and the cylindrical catalyzing body (3030) is installed into acylindrical catalyzing cavity (7035) with the cylindrical catalyzingbody (3030) positioned just above the fuel inlet manifold (3055) and thefuel reactor body (7040) positioned just above the cylindricalcatalyzing body (3030). Each of the fuel reactor body (7040) and thecylindrical catalyzing body (3030) is configured to provide fluidcommunication between the cylindrical fuel chamber (7005) and the fuelinlet manifold (3055) as shown in FIGS. 4 and 4A and described above.The fuel reactor body (7040) is formed using materials that have acoefficient of thermal conductivity of greater than 100 W/m° K and withsufficient thermal mass to rapidly conduct thermal energy away from theinterface between the reactor shield base wall (7015) and the catalyzingbody (3030).

In the present non-limiting alternate embodiment of the SOFC system(7000) the cylindrical catalyzing cavity (7035) has a side wall formedby an inside diameter of the annular enclosure wall (7060). The insidediameter of the annular enclosure wall (7060) is formed with itslongitudinal central axis disposed coaxial with the central longitudinalaxis (2060). The cylindrical catalyzing cavity (7035) includes two openends each forming a circular aperture with a top circular aperturefacing the disk shaped outer enclosure top end flange (7102) and abottom circular aperture facing the fuel inlet manifold (3055). Theannular enclosure wall (7060) includes an annular seal plate (7105)surrounding the top circular aperture that mechanically interfaces withthe disk shaped outer enclosure top end flange (7102), The annular sealplate (7105) is attached to the disk shaped outer enclosure top endflange (7102) by mechanical fasteners or the like, not shown. An O-ringseal element (7110), or the like, is disposed between the annular sealplate (7105) and the disk shaped outer enclosure top end flange (7102),e.g. in an O-ring groove, and serves to gas seal a top portion of thecylindrical catalyzing cavity (7035).

Disk shaped outer enclosure top end flange (7102) is attached to theouter cylindrical sidewall (2514) and the joint between the two elementsprovides a continuous thermally conductive path. Like the fuel reactorbody (7040) and the other outer enclosure walls (2514) and (2518) theouter enclosure top end flange (7102) is formed from materials that havea coefficient of thermal conductivity of greater than 100 W/m° K andwith sufficient thermal mass to rapidly conduct thermal energy from theinterface between the reactor shield base wall (7015) and the catalyzingbody (3030). As noted above thermal energy absorbed by the outerenclosure top end flange (7102) is rapidly conducted to the outercylindrical wall (2514) to minimize thermal gradients from one area ofthe outer enclosure to another. The disk shaped outer enclosure top endflange (7102) is attached to the outer cylindrical wall (2514) bymechanical fasteners (not shown) by welding, soldering, or the like. Inany case the joint formed between the top end flange (7102) and theouter cylindrical wall (2514) is gas sealed and provides a substantiallycontinuous thermally conductive pathway.

As described above, the reactor shield based wall (7015) is configuredto absorb thermal energy generated within the cylindrical catalyzingbody (3030). The entire fuel reactor body (7040) is configured toprovide a continuous thermally conductive path to the disk shaped topend flange (7102) in order to rapidly conduct thermal energy generatedwithin the cylindrical catalyzing body (3030) to the disk shaped outerenclosure top end flange (7102) and from it to the cylindrical side wall(2514) and outer bottom wall (2518). Thus, a change in the instantaneoustemperature of reactor shield base wall (7015) is rapidly followed by acorresponding change in the temperature of the entire outer enclosure.

8.10 Thermal Energy Transfer from the Hot Zone Enclosure to the OuterEnclosure

As detailed above each wall of the outer enclosure (2514), (2518),(7102) comprises materials having a high coefficient of thermalconductivity, e.g. between 100 and 300 W/m° K and preferably above 140W/m° K. Accordingly, the outer cylindrical side wall (2514), disk shapedouter bottom wall (2518) and disk shaped outer enclosure top end flange(7102) are fabricated from one or more of copper, molybdenum, aluminumcopper, copper nickel alloys, or a combination thereof. Each of thewalls (2514), (2518) and (7102) preferably comprises aluminum or analuminum alloy preferably having a coefficient of thermal conductivityabove 140 W/m° K and each having sufficient thermal mass, i.e. thicknessto rapidly conduct thermal energy throughout its volume and from oneadjoining wall to another. In the present non-limiting exampleembodiment, the outer cylindrical wall (2514) and the disk shaped outerbottom wall (2518) have a material thickness in a range of 0.5-6.5 mm(0.20-0.25 inches) and the outer enclosure top end flange (7102) has amaterial thickness in a range of 4.0-10.0 mm (0.16-0.39 inches);however, other thickness ranges are usable without deviating from thepresent disclosure.

Specifically, each of the outer enclosure walls (2514, 2518, 7102) isconfigured to provide a substantially continuous thermally conductivepathway for rapid conduction of thermal energy by thermal conductionfrom one area of the outer enclosure to another in order to more rapidlyreduce temperature gradients between regions of the outer enclosure suchthat the entire outer enclosure wall structure remains substantially atthe same uniform temperature throughout.

As further described above the hot zone enclosure walls (2015, 2016, and2017) and (2214 and 2080) form a continuous thermally conductive pathwaysuitable for rapid thermal conduction from one area of the hot zoneenclosure walls to another in order to more rapidly reduce temperaturegradients between the hot zone enclosure walls and maintain the entirehot zone enclosure wall structure substantially at the same temperature.The intermediate enclosure walls (2510, 2511, and 2513) are thermallyconductively coupled with the hot zone enclosure walls by the diskshaped end wall (2017). As detailed above each of the intermediateenclosure walls comprises a material having a thermal conductivity ofless than about 25.0 W/m° K, as compared with the coefficient of thermalconductivity of the hot zone enclosure walls which is 100 W/m° K orhigher. Additionally, the disc shaped walls (2017, 2084 and 2214)provide a greater thermal mass as compared with less thermal massprovided by the intermediate enclosure walls. As a result, the hot zoneenclosure walls absorb and conduct thermal energy at a faster rate thanthe intermediate enclosure walls. While the hot zone enclosure walls arethermally conductively connected to the intermediate enclosure walls bythe disk shaped wall (2017), the thermal mass of the connection ispurposely made small in order to slow a conductive heat flow rate acrossthe thermally conductive path formed by the wall (2017). This provides athermal gradient between the hot zone enclosure walls and theintermediate enclosure walls. The benefit of the thermal gradientprovided between the hot zone enclosure walls and the intermediateenclosure walls is an increase in thermal radiation being emitted fromthe hot zone enclosure walls to more rapidly heat incoming cathode airin the recuperator chamber (2210) and air present in the cathode chamber(2010).

As further detailed above each wall of the outer enclosure (2514, 2518,and 7102) comprises materials having a high coefficient of thermalconductivity, e.g. between 100 and 300 W/m° K and preferably above 140W/m° K. Accordingly, the outer cylindrical side wall (2514), disk shapedouter bottom wall (2518) and disk shaped outer enclosure top end flange(7102) are fabricated from one or more of copper, molybdenum, aluminum,nickel or alloys thereof. In one non-limiting embodiment the walls(2514, 2518, 2516 and 7102) preferably comprises aluminum or an aluminumalloy preferably having a coefficient of thermal conductivity above 140W/m° K. Additionally, each of the walls (2514, 2518, 2516, and 7102) isformed with sufficient thermal mass, i.e. thickness or total volume, torapidly conduct thermal energy throughout its volume, e.g. from oneadjoining outer enclosure wall to another. In the present non-limitingexample embodiment shown in FIGS. 3 and 7, the outer enclosure walls(2514 and 2518) have a material thickness in a range of 0.5-6.5 mm(0.02-0.25 inches) and the wall (7102) has a material thickness in arange of 4.0-10.0 mm (0.16-0.39 inches; however other thickness rangesare usable without deviating from the present disclosure. In the presentnon-limiting example embodiment shown in FIGS. 2 and 7, the hot zonewalls (2015) and (2016) have a material thickness in a range of 0.5-13mm (0.02-0.5 inches), however other thickness ranges are usable withoutdeviating from the present disclosure.

A layer of thermal insulation (2512) is disposed between outsidesurfaces of the intermediate enclosure walls and the inside surfaces ofouter enclosure walls. Preferably, the layer of thermal insulation(2512) is constructed to ensure that surfaces of the outer cylindricalside wall (2514), the disk shaped outer bottom wall (2518), and the diskshaped outer enclosure top end flange (7102) remain within a desiredoperating temperature range e.g. 95-110° C.

The annular enclosure wall (7060) comprises a high temperature resistantmaterial such as Hastelloy or Monel which each have a high nickelcontent to resist oxidation damage and which each have suitable servicetemperatures ratings, e.g. exceeding 400° C. However, both Hastelloy andMonel have a coefficient of thermal conductivity of less than about 25.0W/m° K. Additionally, the annular enclosure wall (7060) is formed with awall thickness in the range of 0.02 to 0.1 inches, but in any case, thethickness of the annular enclosure wall (7060) is selected to provide alower thermal mass than a thermal mass of the thermally conductive wallsof the hot zone enclosure in order to reduce the relative thermal massof the annular enclosure wall (7060) as compared to the thermal mass ofthe hot zone enclosure walls and the intermediate enclosure walls. Thus,due to its lower thermal conductivity and reduced thermal mass, theannular enclosure wall (7060) resists conductive thermal energy transferbetween the hot zone enclosure walls and the outer enclosure walls inorder to maintain a thermal gradient between the hot zone enclosurewalls and the outer enclosure walls. However, this resistance toconductive thermal energy transfer by the annular enclosure wall (7060)merely reduces the rate of thermal conductance or the heat flow ratefrom higher temperature hot zone enclosure walls to the lowertemperature outer enclosure walls. More specifically the configurationof the annular enclosure wall (7060) provides a thermal gradient betweenthe hot zone enclosure walls and the hot zone enclosure walls.

8.11 Over-Temperature Protection System

Potentially dangerous and harmful over temperature conditions can occurdue to excessive heat generation at various locations within the SOFCsystem (7000). During operation over temperature conditions can occur inthe cell stack (2005), within cylindrical catalyzing body (7030) and atother locations such as inside or proximate to the combustion chamber(2135), inside or proximate to the cold start combustion chamber (2300)and or inside the air gap (2155).

Over temperature conditions can escalate rapidly and lead to acatastrophic failure such destruction of the SOFC fuel cells and or anexplosion or fire. An over temperature condition often leads to a burnthrough wherein metal walls are partially melted or otherwise damagedand the insulation layer (2512) is destroyed or rendered permanentlyless effective. A catastrophic failure may include fuel combustionwithin the cylindrical fuel chamber (3005) where fuel combustion is notintended to occur. Thus, when an over temperature condition occursanywhere with the SOFC system it is desirable to stop fuel from enteringinto to the SOFC system (7000) as quickly as possible before the overtemperature condition leads to a catastrophic failure or causes damageto the SOFC system.

Conventional SOFC systems monitor internal temperatures using internaltemperature sensors. Temperate sensors are positioned inside the SOFCsystem proximate to critical areas where an over-temperature or anunder-temperature condition can adversely affect the performance of theSOFC system. Each internal temperature sensor is in communication withan electronic controller over a wire communication interface. Theelectronic controller interprets temperature signals received frominternal temperature sensors and runs software or other logical processsteps to monitor and log temperature sensor inputs. Generally, theelectronic controller (190) stores temperature limit ranges in a memorymodule wherein each temperature limit range relates to a differentoperating mode and or a different internal sensor location. One problemwith internal temperature sensors is that if they fail they are not easyto replace. Additionally, internal temperature sensors of an SOFC systemare in a high temperature and often contaminated environment that canreduce the useful life of the sensors. There is a need in the art to useexternal temperature sensors to determine SOFC temperature levels andpreferably to a single external temperature sensor to determine a singleinstantaneous SOFC surface temperature that can be used to triggervarious SOFC system process controls.

According to the present disclosure process controls can be triggered bychanges in a temperature being monitored by a single externaltemperature sensor. In one example embodiment described above theoperation of the air moving device (3130) shown in FIG. 3 is responsiveto variations in temperature of an external surface of the SOFC system(3000). In particular, the electronic controller (190) using temperaturesensor signals from an external temperature sensor (3135) toggles theair moving device (3130) on or off in response to instantaneoustemperature variation as indicated by the external temperature sensor(3135).

Referring to FIG. 7 the SOFC system (7000) includes an externaltemperature sensor (7135) mounted in contact with an external surface ofthe disk shaped outer enclosure top end flange (7102). Alternately theexternal temperature sensor (7135) can be mounted in contact with anyexternal surface of the outer enclosure walls. The external temperaturesensing element (7135) is in communication with the electroniccontroller (190) and delivers a temperature signal to the electroniccontroller (190) over a communication pathway (7140). In variousembodiments the SOFC system (7000) may also be equipped with the airmoving element (3130), shown in FIG. 3 and described above, which isoperable by the electronic controller (190) to move air over the diskshaped outer enclosure top end flange (7102) in order to reduce itstemperature.

In an example operating mode, the electronic controller (190) receivestemperature signals from the external temperature sensing element (7135)over communication pathway (7140) and determines an instantaneoustemperature of the external surface that the external temperaturesensing element is mounted to. If the instantaneous temperature is notwithin an expected temperature range, the electronic controller isprogrammed to use software and or other logical operators to carry outvarious operating procedures in response to out of range instantaneoustemperature values.

In a first instance the SOFC system is operating in a normal operatingmode generating DC output power and with a steady uniform flow of inputfuel air mixture entering the fuel chamber (7005) from the fuel inputmodule (197), shown in FIG. 1.

Fuel input module (197) includes an operable fuel supply valve (7610).The operable fuel supply valve is disposed along the fuel input conduit(7045) between a fuel source and the fuel reformer (7020). The operablefuel supply valve is in communication with the electronic controller(190) over a communication channel (7666) and with an electrical powersource, not shown, over a power conduit (7830). The operable fuel supplyvalve (7610) has a default state wherein the valve is closed, e.g. heldclosed by a spring force, or the like. The valve is operated by theelectronic controller (190) to open by overcoming the spring force whena power signal is applied to an actuator incorporated within orotherwise associated with the valve.

In one non-limiting embodiment the electronic controller (190) causes apower signal to be applied to the valve actuator to overcome the springforce and open the fuel supply valve (7610). Depending on an amplitudeof the power signal the valve may be opened slightly, e.g. at athreshold power signal amplitude, or the valve may be fully opened, e.g.at a maximum power signal amplitude. In operation, the electroniccontroller (190) is operable to vary the power signal amplitude in amanner that moves the valve actuator to various open positions rangingbetween slightly or partially open to fully opened in response tochanges in the amplitude of the power signal being delivered to thevalve actuator. The electronic controller (190) operates to modulate amass or volume flow rate of the fuel air mixture (3025) that is passingthrough the input conduit (7045) into cylindrical fuel chamber (7005) byvarying the amplitude of the power signal on the power conduit (7830).

In an operating mode of the present disclosure, the electroniccontroller (190) monitors the external temperature sensing element(7102) to determine an instantaneous temperature of the disk shaped topend flange (7102). A software program or other logical operatorsoperating on the electronic controller (190) compares the measuredinstantaneous temperature of the top end flange with a temperature rangeassociated with the current operating mode of the SOFC system.Temperature ranges for different operating modes are stored on a memoryassociated with the electronic controller (190). Non-limiting exampleoperating modes include a startup operating mode when the cold startcombustion chamber (2300) is in use, a steady state operating modewherein the cold start combustion chamber is not in use and otherswherein an input flow rate of incoming fuel is modulated to provide moreor less DC power output from the fuel stack.

In each case if the instantaneous temperature sensed by the externaltemperature sensing element (7102) is within the temperature rangeexpected the electronic controller takes no action. However, if theinstantaneous temperature sensed by the external temperature sensingelement (7102), i.e. the temperature of the top end flange (7102) is notwithin the temperature range expected actions may be taken by theelectronic controller (190).

As a safety feature the expected temperature range for any of theoperating modes has an upper limit called the “controller failsafetemperature”. In the present non-limiting example operating mode, thecontroller failsafe temperature is 140° C. In particular if theinstantaneous temperature measured by the external sensor (7135) is 140°C. or higher the electronic controller initiates a safety shut downprocedure than at least includes de-energizing the operable fuel supplyvalve (7610) actuator to prevent any further fuel flow into the SOFCsystem.

Once the controller failsafe temperature is sensed, the electroniccontroller initiates software or logically controlled shutdown processthat includes commanding the fuel delivery module (197) to close thefuel supply valve (7610) by cutting power thereto. Additionally, thecontrolled shut down process may include ceasing fuel delivery to thecold start combustion chamber (2300), ceasing air input by the air inputmodule (198) and actuating the air moving device (3210), if the SOFCsystem is so equipped and if the air moving device is not alreadyoperating.

More generally, due to the thermally conductive pathway and relativelyhigh thermal conductivity provided by the improved outer enclosure ofthe present disclosure a single external temperature sensing element(7135) positioned on any surface of the outer enclosure eccentricallysenses an instantaneous temperature of the entire outer enclosure walls(132).

In a further aspect of the present disclosure a thermal fuse (7860) thatincludes a fusible link is disposed in contact with an outside surfaceof the disk shaped outer enclosure top end flange (7102), or in contactwith any outer surface of the outer enclosure. The thermal fuse (7860)is disposed along the fuel supply power conduit (7830) between the powersupply of source and the operable fuel supply valve (7610). The thermalfuse (7860) is a passive device and independent of the electroniccontroller (190). The thermal fuse is configured to interrupt electricalpower passing from the supply valve power source, not shown, to theoperable fuel supply valve (7610) when the fusible link melts and causesa short circuit inside the thermal fuse (7860). The fusible link has aspecific melting temperature that is equal to a system failsafetemperature. In the present non-limiting example embodiment, the systemfailsafe temperature is equal to a temperature greater than thecontroller failsafe temperature. In one non-limiting exemplary operatingmode the system failsafe temperature is 180° C. In particular, if thetemperature of the fusible link reaches the system failsafe temperatureof 180° C. the fusible links melts and this causes a short circuitacross the thermal fuse (7860). The short circuit cause a zero poweramplitude at the operable valve (7610) which closes. Thus, fuel flow tothe fuel chamber (7005) is prevented. In an exemplary, non-limitingembodiment, thermal fuse (7860) includes a commercially availablethermal fuse, e.g., any one of Tamura LE series, NEC Sefuse SF series,Microtemp G4A series, and Hosho Elmwood D series thermal fuses whereinthe selected fuse is configured with a fusible link that melts at thedesired system failsafe temperature.

As set forth above, the system (7000) includes the electronic controller(190) which is operable to carry out a software or logical shut downprocedure when the single external temperature sensor (7135) reports aninstantaneous temperature equal to the controller failsafe temperature.The software or logical shut down procedure at least includes causingthe operable fuel supply valve (7610) to close using logical commands.Meanwhile in the event that the fusible link of thermal fuse (7860)reaches the system fails safe temperature the thermal fuse preventspower from reaching the operable fuel supply valve (7610) such that fuelflow to the fuel chamber is stopped in the event that the fuel flow wasnot previously stopped by the software or logical shut down procedure.

As noted above because each of the outer enclosure walls (2514, 2518,and 7102) is configured to provide a thermally conductive pathway with ahigh coefficient of thermal conductivity the entire outer enclosure wallstructure rapidly reaches thermal equilibrium at substantially at thesame instantaneous temperature. Accordingly, the temperature sensingelements (7135) and the thermal fuse (7860) can be positioned on anyoutside surface of the outer enclosure including on different outsidesurfaces of the outer enclosure. Moreover, as detailed above, theinstantaneous temperature of the outer enclosure increases and decreasesin response to increases and decreases in the temperature of the hotzone enclosure walls which are thermally conductively connected over theannular enclosure wall (7060). Thus, any prolonged increase ininstantaneous temperature at any location within the SOFC system (7000)ultimately leads to an increase in temperature of the outer enclosurewalls which is then detected by the external temperature sensing element(7135) and monitored by the electronic controller (190).

8.12 Fuel/Oxidant Input Control Module

Referring now to FIG. 8, a schematic representation of a furthernon-limiting exemplary embodiment of a Solid Oxide Fuel Cell (SOFC)system (8000) according to the present disclosure is illustratedtherein. The SOFC system (8000) includes a fuel/oxidant input controlmodule (8005), also shown as the fuel input module (197), in FIG. 1. Thefuel/oxidant input control module (8005) includes, or is fluidly coupledwith each of, an oxidant supply source (8010) and a hydrocarbon fuelsupply source (8020). The oxidant supply source (8010) is in fluidcommunication with a mixing chamber (8015), e.g. a spiral mixingchamber, by a connecting oxidant input conduit (8017). The fuel supplysource (8020) is in fluid communication with the mixing chamber (8015)by a connecting fuel input conduit (8022). An oxidant flow modulator(8025) is disposed along the oxidant input conduit (8017) between theoxidant supply source (8010) and the mixing chamber (8015). Ahydrocarbon fuel flow modulator (8035) is disposed along the fuel inputconduit (8022) between the hydrocarbon fuel supply source (8020) and themixing chamber (8015). Each flow modulator (8025, 8035) includes atleast one electro-mechanical actuator, not shown, controlled by theelectronic controller (190). The electronic controller (190) isconfigured to independently modulate an input oxidant flow rate and aninput hydrocarbon fuel flow rate to the mixing chamber (8015). Each ofthe input oxidant flow rate and the input hydrocarbon fuel flow rate canbe modulated between a substantially zero input flow rate and a maximuminput flow rate. In alternate embodiments, the mixing chamber (8015) iseliminated and each of the oxidant input conduit (8017) and the fuelinput conduit (8022) is connected between the corresponding supplysource and the fuel chamber (3005), that is formed inside the fuelreactor system (3000), shown in FIGS. 3, 4, 4A and 7.

8.12.1 Compressed Gas Container

In one non-limiting exemplary embodiment, one or both of, the oxidantsupply source (8010) and the hydrocarbon fuel supply source (8020), is acompressed gas container, e.g. a pressurized oxygen or air container, ora pressurized hydrocarbon fuel container. In either case, thepressurized container includes a passive pressure regulator, not shown.The passive pressure regulator is disposed between the compressed gascontainer and the mixing chamber (8015) and operates to pressuremodulate or regulate a flow of high pressure gas exiting from thecompressed gas container. A flow of lower pressure gas is released, bythe pressure regulator, into the corresponding input conduit (8017,8022), wherein the lower pressure gas is released at a much lower gaspressure as compared with the high-pressure gas stored inside thecompressed gas container. The passive pressure regulator also acts as apassive gas flow modulator. This occurs when the lower pressure gasexiting from the corresponding input conduit (8017, 8022), to the mixingchamber (8015), causes the gas pressure inside the corresponding conduitto drop. In response to the drop in gas pressure, inside thecorresponding conduit, the passive pressure regulator releases gas fromthe pressurized gas container into the corresponding conduit, until thegas pressure inside the corresponding conduit is restored to a setpressure of the passive gas regulator. Thus, a gas flow rate exitingfrom either one of the input conduits (8017, 8022), e.g. to the mixingchamber (8015), is replaced by a corresponding gas flow rate beingreleased by the corresponding passive pressure regulator. Accordingly,each gas regulator operates to maintain a constant gas pressure insidethe corresponding input conduit (8017, 8022).

8.12.2 Air Pump/Fan

In another non-limiting exemplary embodiment, the oxidant source (8010)is an air pump or a fan that draws air into the oxidant input conduit(8017) from the surrounding environment or from an air intake vent, orthe like. In one non-limiting exemplary embodiment, the air pump or afan is also operated as the oxidant flow modulator (8025) when the airpump or fan includes a controllable electro-mechanical actuator incommunication with the electronic controller (190). The controllableelectro-mechanical actuator, not shown, operates to rotate or otherwisemove the controllable air moving device, e.g. a pump vane, a fan blade,or the like, associated with the air pump or fan. Movement of the airmoving device directs or draws the oxidant into the oxidant inputconduit (8017) and the oxidant fuel flow rate is varied by varying avelocity of the air move device, e.g. by varying an angular velocity ofa rotating pump vane or fan blade. The changes in velocity of the airmoving device are driven by control and command signals received fromthe electronic controller (190). The command and control signalsreceived by the air moving device modulate a velocity of the air movingdevice which corresponds with modulating a flow rate of the air passingthrough the oxidant input conduit (8017) to the mixing chamber (8015).The air pump or fan, when operating as the oxidant flow modulator(8025), is controlled by the electronic controller (190) and is operatedto modulate a fluid flow rate of the air passing through the oxidantinput conduit (8017) to the mixing chamber (8015) between asubstantially zero oxidant flow rate and a maximum oxidant flow rate.

In a further non-limiting embodiment, the oxidant source (8010) is anair pump or a fan that draws air into the oxidant input conduit (8017)from the surrounding environment or from an air intake vent, or thelike, at a substantially constant air flow rate and the air flow ratemodulation is performed by a gas control valve, described below.

8.12.3 Liquid Fuel Supply

In another non-limiting exemplary embodiment, the hydrocarbon fuelsupply source (8020) comprises a liquid hydrocarbon fuel, e.g. kerosene,gasoline, or the like. In this embodiment, the hydrocarbon fuel supplysource (8020) comprises a liquid fuel container, which may bepressurized, and a vaporizer or atomizer module disposed between theliquid fuel container and the mixing chamber (8105). The liquid fuel isdelivered into the vaporizer or atomizer which is configured to convertthe liquid fuel into hydrocarbon gas vapor or a mist comprising liquidfuel droplets. The hydrocarbon gas vapor or mist is delivered into thehydrocarbon fuel input conduit (8022) for delivery to the mixing chamber(8015). In the present embodiment, the vaporizer or atomizer may also beoperated as the hydrocarbon fuel flow modulator (8035) when thevaporizer or atomizer includes a controllable electro-mechanicalactuator, or the like, in communication with the electronic controller(190). The controllable electro-mechanical actuator operates to move orotherwise manipulate an element associated with vaporizing or atomizingthe liquid fuel supply to modulate the hydrocarbon fuel flow rate to themixing chamber (8015).

In a further non-limiting embodiment, the vaporizer or atomizer deliversa liquid hydrocarbon fuel mist or vapor into the hydrocarbon fuel inputconduit (8022) from the liquid fuel source at a substantially constanthydrocarbon fuel flow rate and the hydrocarbon fuel flow rate modulationis performed by a gas flow control valve, described below.

8.12.4 Gas Flow Control Valve

In a further non-limiting exemplary embodiment, one or both of theoxidant flow modulator (8025) and the hydrocarbon fuel flow modulator(8035) comprises a gas flow control valve, disposed along thecorresponding input conduit (8017, 8022), between the correspondingoxidant supply source (8010) or hydrocarbon fuel supply source (8020)and the mixing chamber (8015). Each gas flow valve includes anelectro-mechanical actuator in communication with the electroniccontroller (190). The electro-mechanical actuator operates to rotate orotherwise move a movable gate, or the like, wherein the movable gate isdisposed inside the gas flow control valve or inside the correspondinginput conduit (8017, 8022). The movable gate is moved in response tocontrol and command signals received from the electronic controller(190) to independently modulate a flow rate of each of the oxidant andthe hydrocarbon fuel passing through the gas control valve to the mixingchamber (8015). Accordingly, each of the gas flow valves operating aseither the oxidant flow modulator (8025) or the fuel flow modulator(8035), is operated by the electronic controller (190) and theelectronic controller is configured to modulate a fluid flow rate,passing through the movable gate, wherein the fluid flow rate rangesbetween a substantially zero oxidant or hydrocarbon fuel flow rate, anda maximum oxidant or hydrocarbon fuel flow rate. Preferably, the gasflow valve is operable to provide a plurality of discreet incrementalvolumetric flow rate levels over the flow rate range with eachincrementally volumetric flow rate level varying the flow rate betweenabout 0.1 and 1.0 standard cubic centimeter per minute, (SCCM).

8.12.5 Cathode Air Pump

The fuel cell stack includes a cathode air input port (2205) that leadsinto the cathode chamber (2010), shown in FIG. 2. A cathode air or otheroxidant source (8045) is disposed to deliver a cathode air flow, orother oxidant flow, into a cathode air input conduit (8055) that leadsto the air input port (2205). A cathode air flow modulator (8050) isdisposed along the cathode air input conduit (8055) between the cathodeair source (8045) and the cathode air input port (2205). The cathode airflow modulator (8050) includes at least one controllableelectro-mechanical actuator, not shown, that is controlled by theelectronic controller (190). In one exemplary embodiment, the cathodeair source (8045) is an air pump or a fan that is also operated as thecathode flow modulator (8050). In this example, the air pump or fanincludes a controllable electro-mechanical actuator in communicationwith the electronic controller (190). The controllableelectro-mechanical actuator operates to rotate or otherwise move thecontrollable air moving device, e.g. a pump vane, a fan blade, or thelike, associated with the air pump or fan, at different velocities.Movement of the air moving device directs or draws cathode air into thecathode air input conduit (8055) and a volumetric flow rate of thecathode air is varied by varying a velocity of the air move device, e.g.by varying an angular velocity of a pump vane or fan blade. The changesin velocity of the air moving device are driven by control and commandsignals received from the electronic controller (190). The command andcontrol signals drive changes in velocity of the air moving device tomodulate the volumetric flow rate of the cathode air passing throughcathode air input conduit (8055) to the cathode air input port (2205).Accordingly, the air pump or fan, operating as the cathode flowmodulator (8050), is operated by the electronic controller (190) and theelectronic controller is configured to modulate the volumetric fluidflow rate of the cathode air passing through the cathode air inputconduit (8055) to the cathode air input port (2205) between asubstantially zero cathode air flow rate, and a maximum cathode air flowrate. Preferably, the air moving device used to modulate the volumetricflow rate of the cathode air provides a plurality of discreetincremental volumetric flow rate levels over the volumetric flow raterange with each incrementally volumetric flow rate level varying theflow rate between about 0.5 and 2.0 standard cubic centimeter perminute, (SCCM).

As described above, with respect to the oxidant supply source (8010),the cathode air supply source (8045) may comprise a compressed gascontainer, e.g. a pressurized oxygen or air tank, that includes apassive pressure regulator. Alternately, the cathode supply source(8045) may comprise an air pump or a fan that draws air into the cathodeair input conduit (8055) from the surrounding environment or from avented conduit, or the like. However, the air pump or fan is notoperated as the cathode air flow modulator (8050). Instead, the flowrate of the cathode air that is delivered into the cathode air conduit(8055) by the air pump or fan is substantially constant when the airpump or fan velocity is not modulated by the electronic controller. Inthis embodiment, the fuel flow modulation is performed by a gas flowcontrol valve disposed along the fuel input conduit (8022), as describedabove.

8.12.6 Fuel Air Mixture

The mixing chamber (8015) is preferably a spiral chamber used to mix thehydrocarbon fuel flow with the oxidant flow to generate a fuel airmixture (2025, 3025). The fuel air mixture preferably has an oxygen tocarbon (O:C) ratio in a range of 1.0 to 2.2 wherein the O:C ratiocorresponds with a molar ratio, e.g. the ratio of oxygen atoms to carbonatoms.

The fuel air mixture (2025, 3025) exits from the mixing chamber (8015)to the gas flow conduit (2045 7045), which extends from the fuel/oxidantinput control module (8005) to the fuel chamber (3005), that is formedinside the fuel reactor system (3000), shown in FIGS. 3, 4, 4A and 7,and described above. While the preferred hydrocarbon fuel of the presentdisclosure is methane (CH₄), other longer hydrocarbon molecule chainscan be used including ethane (C₂H₆) propane (C₃H₈), butane (C₄H₁₀), orthe like. Additionally, liquid hydrocarbon fuels having hydrocarbonchains ranging between C₅H₁₂ through C₁₈H₃₂ can be reformed by thesystems and methods of the present disclosure.

8.12.7 CPOX Reaction

The fuel reactor system (3000) is configured to reform the fuel airmixture (2025, 3025) by Catalyst Partial Oxidation (CPOX). The CPOXreaction is an exothermal reaction, (flameless combustion), thatconverts the fuel air mixture to syngas (2027). The syngas (2027) is areformate that includes the anode gas that is used to react with thesolid oxide anode electrode surfaces formed onto inside surfaces of eachtubular fuel cell (2080), of the SOFC stack (135, 2005). The anode gasreactants are H₂ and CO, because both reactants are capable of bondingwith oxygen atoms that are available on the solid oxide anode electrodesurfaces. The bonding of oxygen atoms or ions, available on the anodeelectrode surface, with the H₂ reactant, to form H₂O, and with the COreactant to form CO₂, generates the DC current that is output from eachof the tubular fuel cells (2080) to the DC power module (140) shown inFIG. 1. In alternate embodiments, the CPOX reactor and fuel reformingmethods of the present disclosure are usable to deliver syngas to planarsolid oxide anode electrode surfaces without deviating from the presentdisclosure.

The oxygen atoms, or ions, that are available on the solid oxide anodeelectrode surfaces are received from oxygen gas O₂ available from thecathode air that is pumped into the cathode chamber (2010). The inputvolumetric flow rate of the cathode air is modulated to keep up with thedemand for oxygen atoms or ions on the solid anode electrode surfaces.Oxygen gas from the cathode air reacts with the solid oxide cathodeelectrode surfaces (155), formed onto outside surfaces of each tubularfuel cell (2080), or onto planar solid oxide cathode electrode surfaces.The oxygen gas O₂, is separated in to individual oxygen atoms, or ions,that pass through the solid oxide cathode electrode, through theelectrolyte layer disposed between the cathode electrode and the anodeelectrode, and through the solid oxide anode electrode that is exposedto the anode gas.

Equation 6, listed below, details the CPOX chemical reaction associatedwith converting the fuel air mixture to syngas (2027). The CPOX chemicalreaction of equation 6 is initiated when the fuel air mixture contactsthe catalyst layers (3090) coated on inside surfaces of the catalystfuel passages. The catalyst layers (3090) initiate the CPOX chemicalreaction at a CPOX reaction temperature of 600 to 900° C. Without thecatalyst layers (3090) the CPOX reaction temperature would be 1000 to1200° C.

C_(n)H_(m)+(n/2)O₂ →nCO+m/2H₂  EQU. 6

Based on Equation 6, when the hydrocarbon fuel is methane, (CH₄), thefuel air mixture has an O:C ratio equal to 1.0 and an output ratio ofCO:H₂ of 0.5. When the hydrocarbon fuel is ethane, (C₂H₆), the fuel airmixture has an O:C ratio equal to 1.0 and an output ratio of CO:H₂ of0.66. When the hydrocarbon fuel is propane, (C₃H₈), the fuel air mixturehas an O:C ratio equal to 1.0 and an output ratio of CO:H₂ of 0.75.

However, nothing in equation 6 accounts for the use of air as theoxidant, instead of pure oxygen, or for using a non-homogeneoushydrocarbon fuel source that includes a mixture of hydrocarbon moleculesof varying chain length, and/or other contaminants. Moreover, Equation 6assumes exact molar ratios of the reactants, which in practice isdifficult to achieve. Without exact molar ratios of the fuel airmixture, the syngas reaction can be incomplete. In one case, when thefuel air mixture has a low O:C ratio, e.g. less than 1.0, i.e., thereare more hydrocarbon fuel molecules than there are available oxygenmolecules to react with and the syngas may include unreacted hydrocarbonfuel molecules CnHm. When this occurs, the unreacted hydrocarbon fuel isflushed from the fuel cells without having generated any electricalpower. In the other case, when the fuel air mixture has a high O:Cratio, greater than 1.0, i.e., there are more oxygen molecules thanhydrocarbon fuel molecules, the syngas includes excess oxygen gas (O₂)that can bond with the H₂ and CO components of the syngas, therebyreducing the anode gas reactants that are available to contribute toelectrical power generated. Thus, an important aspect of the presentdisclosure is to balance the components of the fuel air mixture ofEquation 6 to provide an O:C ratio that eliminates unreacted hydrocarbonfuel, e.g. free carbon atoms and excess oxygen gas from the syngas whichcan react to form methane, (CH₄). As described below, the presentdisclosure uses the eliminating methane from the syngas formed by theCPOX reaction as a control indicator for establishing a desirable O:Cratio.

Other known problems associated with the CPOX chemical reaction include,coke formation, and undesirable reactions with fuel contaminates. Cokeformation results when carbon molecules bond with surfaces of thecatalyst layers (3090) during the CPOX reaction. Carbon molecules, thatare contained in the syngas output, can also contaminate surfaces of thesolid oxide anode electrode layers (150), which reduces efficiency ofthe anode electrode layer. In both instances, coke formation tends toreduce the overall efficiency of the SOFC system. As also noted above,low O:C ratio may further contribute to unreacted hydrocarbon atomsand/or free carbon atoms that can participate in coke formation.

Coke formation is temperature dependent and tends to be morethermodynamically favorable at CPOX reaction temperatures that are belowabout 800° C. Thus, it is important to maintain a minimum CPOX reactiontemperature of about 800° C. and preferability above about 850 to 950°C. to avoid coke formation. As described above, the maximum CPOXreaction temperature occurs proximate to the interface (3032) where theincoming fuel air mixture makes initial contact with the catalyzinglayer. However, a portion of the fuel air mixture makes initial contactwith the catalyzing layer more distal from the interface layer (3032),and likely reacts at a lower CPOX reaction temperature than the CPOXreaction temperature at the interface. Thus, maintaining a minimum CPOXreaction temperature of about 800° C. proximate to the interface (3032)will not necessarily eliminate coke formation distal from the interface(3032), where the reaction temperature may be less than 800° C. Cokeformation is also stimulated by a low O:C ratio, e.g. less than 1.0,however, when the oxidant is air, the actual O:C ratio of the fuel/airmixture exiting the mixing chamber is somewhat uncertain, so it isdesirable to provide another indicator, e.g. the lack of or theminimization of methane in the syngas as an indication that a desiredO:C ratio is being provided.

A CPOX reaction control method is described and addressed in U.S. Pat.No. 8,337,757 to Roychoubhury et al., entitled Reactor Control Method.Roychoubhury et al. disclose a CPOX reactor control method that includesperiodically measuring a CPOX reaction temperature at three separatelocations of the CPOX reactor. The reactor control method includesselecting a steady state operating temperature and a maximum safeoperating temperature. Based on the CPOX reaction temperature measuredin each of the three separate locations, the reactor control methoddetermines a maximum temperature, a minimum temperature and a differencebetween the maximum and minimum temperature. The reactor control methodthen varies three control parameters to change the O:C ratio of theincoming fuel air mixture in a manner that will minimize the differencebetween the maximum and minimum temperature, while preventing themaximum temperature from exceeding the maximum safe operatingtemperature. The three control parameters that are varied to effectivelychange the O:C ratio include, only varying the fuel input flow rate,only varying the air input flow rate, and alternating between varyingthe fuel input flow rate and the air input flow rate.

While Roychoubhury et al. disclose a CPOX reactor control method thataddresses the need to vary the O:C ratio to minimize the differencebetween the maximum and minimum temperature of three separate locationsof the CPOX reactor, one problem with the control method disclosed byRoychoubhury et al. is the need to provide three different thermalsensors with one located at each of the three separate locations in thereactor. Another problem with the CPOX reactor control method, disclosedby Roychoubhury et al., is the failure to consider that modifications tothe O:C ratio used to modify the CPOX reaction temperature can adverselyaffect the SOFC reaction temperature to an extent that an overall powerconversion efficiency of the SOFC system may be compromised.Specifically, when the CPOX reaction temperature alone is used as adesirable O:C ratio indicator, the system power conversion can becompromised. Fuel contaminants such as tar (C₁₀H₈), and other long chainhydrocarbon molecules can participate in coke formation. Sulfur is afuel contaminate that forms sulfides either in the fuel/air mixture orin the syngas. The sulfides, including carbon disulfide (CS₂), hydrogensulfide (H₂S), sulfur dioxide (SO₂), or the like, can poison thecatalyst layers in the CPOX reactor, and can also compete for oxygensites at the solid oxide anode electrode layers (150) in the SOFC stack.Accordingly, it is desirable that the hydrocarbon fuel source have a lowsulfur content, e.g. less than about 50 parts per million (PPM). Anotherproblem that reduces CPOX conversion efficiency is catalyst layer burnthrough, which occurs when portions or the catalyst layers arepermanently damaged by prolonged exposure to excessive reactiontemperatures. For this reason, it is important to prevent a CPOXreaction temperature from exceeding burn through temperatures.

Despite the complexity of syngas generation, when using air as theoxidant, the syngas mainly comprises N₂, H₂ and CO, in varying majorproportions, with a smaller minor proportion of CO₂. However, the weightpercentage of each of the syngas components, including the weightpercentage of the reactants H₂ and CO, varies according to variations inthe O:C ratio, variations in the CPOX reaction temperature, variationsin the hydrocarbon fuel type and variations of the homogeneity andcontaminant content of the hydrocarbon fuel. Accordingly, the syngas mayinclude other components in minor proportions such as, unreactedhydrocarbons, oxygen gas, sulfides, water, or the like, and the weightpercentage of each of the major proportions of syngas components willvary with variations in the O:C ratio of the fuel air mixture and withvariations in the CPOX reaction temperature.

Accordingly, it is an object of one aspect of the present disclosure isto maximize the conversion efficiency of the CPOX reaction by,maximizing a weight percentage of the anode gas reactants H₂ and CO,while also minimizing a weight percentage of unreacted hydrocarbons,e.g. methane (CH₄), and oxygen gas (O₂) in the syngas produced by theCPOX reaction.

8.12.8 First Thermal Sensor and Thermally Conductive Coupling

Turning now to FIGS. 9-12, 13A, 13B and 14, a plurality of differentnon-limiting exemplary embodiments of a first thermal sensor (8030),mounted to a thermally conductive element (9005, 10005, 11005, 12005,13005) are illustrated therein. In each of the non-limiting exemplaryembodiments the corresponding thermally conductive element is supportedin mating contact with a longitudinal surface of the cylindricalcatalyzing body (3030) and is formed from a material that has acoefficient of thermal conductivity of 50 W/m° K, or greater, andpreferably with a coefficient of thermal conductivity of 100 W/m° K orgreater. This compares with a thermal conductivity of the ceramiccatalyzing body of about 2-7 W/m° K. Moreover, each of the thermallyconductive elements is formed with a large enough contact area betweenthe thermally conductive element and the catalyzing body to promote ahigh rate of conductive thermal energy transfer from the catalyzing body(3030) to the thermally conductive element across the contact area. Whenthe temperature difference between the catalyzing body and the thermallyconductive element is large, e.g. at initial startup, the rate ofthermal conduction across the contact area is large. However, as thetemperature difference approaches zero, the largest influences on therate of thermal conduction between the catalyzing body and the thermallyconductive element are, the coefficient of the thermal conductivity ofthe thermally conductive element, the contact area between the thermallyconductive element and the catalyzing body and the thermal mass (seeEQU. 5 above), of the thermally conductive element. However, formaterials such as copper, aluminum and other material having a highcoefficient of thermal conductively, which are mainly metals,differences in thermal mass are more simply represented as difference inmaterial volume. Thus, aside from selecting a material having a highcoefficient of thermal conductivity, the thermally conductive element ofthe present disclosure is formed with sufficient contact area, betweenthe catalyzing body and the thermally conductive element, and withmaterial volume to rapidly conduct thermal energy from the catalyzingbody (3030) to the thermally conductive element. Preferably, the contactsurface area is sized to promote a high enough rate of thermalconductivity between the catalyzing body and the thermally conductiveelement to cause a temperature of the contact area surface to besubstantially matched by a temperature of the thermally conductiveelement.

Each thermally conductive element is supported in mating contact witheither an external or and internal longitudinal surface of thecylindrical catalyzing body (3030). A contact area between thecatalyzing body and the thermally conductive element is defined as aproduct of, a circumferential contact area and a longitudinal contactarea, wherein the longitudinal contact area extends along thelongitudinal axis of the catalyzing body and the circumferential contactarea extends along a circumferential surface of the catalyzing body,which is orthogonal with the longitudinal axis. Other contact areashapes, and orientations are usable without deviating from the presentdisclosure.

When formed with sufficient thermal mass and contact area, the thermallyconductive element is configured to rapidly conduct thermal energyacross the contact area until a temperature of the thermally conductiveelement is substantially equal to an average or bulk surface temperatureof the catalyzing body over the contact surface area. Moreover, based onthe high rate of thermal conduction provided across the contact surfacearea changes in the bulk or average temperature of the contact surfacearea of the catalyzing body are rapidly followed by similar changes intemperature of the thermally conductive element. Accordingly, atemperature sensed by the first thermal sensor (8030) provides areliable and repeatable indicator of the average or bulk surfacetemperature of the catalyzing body over the contact area.

The first thermal sensor (8030) generates a first temperature signal(8031) that is sampled by the electronic controller at a samplingfrequency that generates a continuous stream of first temperature signalvalues each corresponding with an instantaneous temperature of assurface of the thermally conductive element that he first thermal sensoris attached to. Because the temperature sensed by the first thermalsensor (8030) provides a reliable and repeatable indicator of theaverage or bulk surface temperature of the catalyzing body over thecontact area, changes in the first temperature signal (8031) correspondwith proportional changes the CPOX reaction temperature e.g. when theO:C ratio of the incoming fuel is varied. Viewed another way, changes inthe first temperature signal (8031) are proportional to changes in theheat flux density (W/m²) being thermally conducted across the contactarea.

As noted above, a temperature of the CPOX reaction likely varies alongthe longitudinal length of the cylindrical catalyzing body. According toconventional reactor control methods disclosed by Roychoubhury et al.,three temperature sensors are disposed at three separate longitudinalpositions to sense three different temperatures along the longitudinallength of the catalyzing body. An algorithm determines a maximum and aminimum temperature corresponding with the temperature output by thethree sensors and, based on the temperature distribution, the O:C ratioof the incoming fuel air mixture is varied in a manner that minimizesthe difference between the maximum and minimum temperatures sensed bythe three temperature sensors. However, the present disclosure uses onlyone temperature sensor coupled with a thermally conductive elementsupported in contact with the catalyzing body over a contact area thatextends along a portion of the longitudinal dimension of the catalyzingbody. By sensing only, the first temperature signal (8031), the presentdisclosure reduces complexity and improves reliability by reducing thenumber of sensors and eliminating the algorithm for computing thetemperature spread. The thermally conductive element of any of theembodiments shown in FIGS. 9-12 and 13A and 13B is formed from any oneof copper, aluminum, nickel, brass, beryllium, iridium, magnesium,molybdenum, tungsten and zinc and or alloys thereof. Additionally, formaterials that are susceptible to oxidation damage at operatingtemperatures above about 400° C., external surfaces of the thermallyconductive element are coated with an oxidation resistant material, e.g.nickel plating, or the like.

Referring to FIG. 9 in a first exemplary, non-limiting embodiment, afirst thermally conductive element comprises a prismatic rod (9005)disposed in mating contact with an external surface (9010) of thecatalyzing body (3030). A longitudinal axis (9015) of the prismatic rod(9005) is oriented substantially parallel with a longitudinal axis(9020) of the catalyzing body (3030). The catalyzing body (3030) is acylindrical element comprising a ceramic substrate having a diameter of25.4 mm and a longitudinal length of 25.4 mm. The catalyzing body(3030), when installed into the cylindrical catalyzing cavity (3035),has an input end at the interface (3032) and an output end (3034), thatdelivers syngas (2027) into the fuel inlet manifold (3055), shown inFIG. 7.

The prismatic rod (9005), of the first thermally conductive element, hasa diameter of 3.2 mm, which is about one eighth (⅛) the diameter of thecatalyzing body (3030). The prismatic rod (9005) has a longitudinallength of, 6.3 to 12.7 mm, which is about one quarter (¼) to one half(½) of the longitudinal length of the catalyzing body (3030). Theprismatic rod (9005) may be longitudinally positioned to contact theexternal surface (9010) of the catalyzing body (3030) at anylongitudinal position between the input or interface end (3032) and theoutput end (3034). An optimal longitudinal contact position of theprismatic rod (9005) may be determined by experimentation, e.g. duringsystem calibration, or may be determined by support structure, or thelike, provided to support the prismatic rod (9005) in mating contactwith the contact surface. Other prismatic rods (9005) having differentlongitudinal dimensions and outside diameter dimensions are usablewithout deviating from the present disclosure.

The first thermal sensor (8030) is attached to or otherwise supported bythe prismatic rod (9005) to provide a thermally conductive couplingbetween at least one surface of the prismatic rod (9005) and the firstthermal sensor (8030). In the example embodiment of FIG. 9, theprismatic rod (9005) includes a through hole or a blind hole (9025) thatextends along the longitudinal axis (9015) of the prismatic rod. Thefirst thermal sensor (8030) is installed into the through or blind hole(9025) and held in place. Alternately, the first thermal sensor (8030)is thermally conductively coupled to any external or internal surface ofthe prismatic rod (9005) by brazing, by a thermally conductive bondingmaterial, by one or more mechanical fasteners or clamps, or the like.

The prismatic rod (9005) is attached to or otherwise supported in matingcontact with the external surface (9010) of the catalyzing body (3030)by a radially inward pressure force applied by the thermally insulatingelement (3080) disposed inside the catalyzing cavity (3035). As bestshown in FIG. 3, the thermally insulating element (3080) is formed as anannular ring disposed inside the catalyzing cavity (3035) between theannular enclosure wall (3060) and the cylindrical catalyzing body(3030). By installing the prismatic rod (9005) and first thermal sensor(8030) into the catalyzing cavity (3035) between the thermallyinsulating element (3080) and the outside surface of the catalyzing body(3030), the thermally insulating element (3080) provides sufficientradially directed compressive force to support the prismatic rode (9005)in mating contact with the cylindrical catalyzing body (3030). Thecompressive force is sufficient to thermally conductively couple theprismatic rod with the cylindrical catalyzing body (3030) over theentire contact area. Alternately, the prismatic rod (9005) is coupled tothe outside surface of the catalyzing body (3030) by brazing, by athermally conductive bonding material, by one or more fasteners orclamps, or the like. Preferably, the configuration of the prismatic rod(9005), the configurations of the first thermal sensor (8030), thelongitudinal position, between the interface (3032) and the output end(3034), and the contact method used to secure the prismatic rod (9005)against the outside surface of the catalyzing body, provide a firsttemperature signal output from the first thermal sensor (8030) that isrepeatable and sufficiently responsive to temperature changes of thebulk or average temperature of the contact area that are primarilyrelated to changes in the oxidant flow rate being delivered into themixing chamber (8015).

Referring now to FIG. 10, a second thermally conductive elementembodiment (10010) comprises a cylindrical segment (10005). Thecylindrical segment (10005) includes a contact surface area (10008) thatis formed with a radius of curvature that is matched with a radius ofcurvature of the outside circumferential surface of the cylindricalcatalyzing body (3030). The cylindrical segment (10005) includes alongitudinal axis (10015) that is oriented parallel with thelongitudinal axis (10020) of the cylindrical catalyzing body (3030). Thecylindrical segment (10005) is formed from a prismatic rod that has adiameter of about 6.4 mm, which is about one quarter (¼) the diameter ofthe cylindrical catalyzing body (3030). The cylindrical segment (10005)has a longitudinal length of, 6.3 to 12.7 mm, which is about one quarter(¼) to one half (½) of the longitudinal length dimension of thecatalyzing body (3030). The cylindrical segment (10005) may belongitudinally positioned to contact the external surface (10010) of thecatalyzing body (3030) at any longitudinal position between the input orinterface end (3032) and the output end (3034). Other cylindricalsegments (10005) having other rod diameter and longitudinal lengthdimensions are usable without deviating from the present disclosure.

The first thermal sensor (8030) is attached to or otherwise supported bythe cylindrical segment (10005) to provide a first temperature signal(8031) corresponding with a temperature of the cylindrical segments(10005) proximate to a surface of contact therewith. In the exampleembodiment of FIG. 10, the cylindrical segment (10005) includes athrough hole or a blind hole (10025) extending along the longitudinalaxis (10015) thereof and the first thermal sensor (8030) is installedinto the through or blind hole (10025). Alternately, the first thermalsensor (8030) is thermally conductively coupled to any external orinside surface of the cylindrical segment (10005) by brazing, by athermally conductive bonding material, by one or more fasteners ofclamps, or the like.

The cylindrical segment (10005) is attached to or otherwise supported inmating contact with the external surface (10010) of the catalyzing body(3030) by a radially inward pressure force applied by the thermallyinsulating element (3080) disposed inside the catalyzing cavity (3035).As best shown in FIG. 3, the thermally insulating element (3080) isformed as an annular ring disposed inside the catalyzing cavity (3035)between the annular enclosure wall (3060) and the cylindrical catalyzingbody (3030). By installing the cylindrical segment (10005) and firstthermal sensor (8030) into the catalyzing cavity (3035), between thethermally insulating element (3080) and the outside surface of thecatalyzing body (3030), the thermally insulating element (3080) providessufficient radially directed compressive force to support thecylindrical segment (10005) in mating contact with the cylindricalcatalyzing body (3030). The compressive force is sufficient to thermallyconductively couple the cylindrical segment (10005) with the cylindricalcatalyzing body (3030) over the entire surface contact area (10008).Alternately, the cylindrical segment (10005) is coupled to the outsidesurface of the catalyzing body (3030) by brazing, by a thermallyconductive bonding material, by one or more fasteners or clamps, or thelike. Preferably, the configuration of the cylindrical segment (10005),the configurations of the first thermal sensor (8030), the longitudinalposition, between the interface (3032) and the output end (3034), andthe contact method used to secure the cylindrical segment (10005)against the outside surface of the catalyzing body, provide a firsttemperature signal output from the first thermal sensor (8030) that isrepeatable and sufficiently responsive to temperature changes of thebulk or average temperature of the contact area that are primarilyrelated to changes in the oxidant flow rate being delivered into themixing chamber (8015).

Referring now to FIG. 11, in a third exemplary, non-limiting embodiment,a third thermally conductive element comprises a hollow cylinder (11005)having an inside diameter that is sized to provide mating contact withthe outside diameter of the catalyzing body (3030) and having an outsidediameter sized to provide a desired thickness, or material volume, ofthe annual wall formed by the hollow cylinder (11005). The hollowcylinder (11005) has a longitudinal axis (11015) that is orientedsubstantially coaxial with the longitudinal axis (11020) of thecatalyzing body (3030). The contact area between the hollow cylinder(11005) and the catalyzing body (3030) extends over the surface of theinside diameter of the hollow cylinder (11005).

The hollow cylinder (11005), is formed with an annular wall thickness ofabout 1.6 mm and a longitudinal length 6.3 to 12.7 mm, that is about onequarter (¼) to one half (½) of the longitudinal length of the catalyzingbody (3030). The hollow cylinder (11005) may be longitudinallypositioned to contact the external surface (10010) of the catalyzingbody (3030) at any longitudinal position between the input of interfaceend (3032) and the output end (3034). The hollow cylinder (11005) isheld in mating contact with the external surface (11010) of thecatalyzing body (3030) by soldering, by a thermally conductive bondingmaterial, by crimping, by fasteners or clamps, by an interference fit,or the like. Other hollow cylinder (11005) having a differentlongitudinal length or material thickness are usable without deviatingfrom the present disclosure.

The first thermal sensor (8030) is attached to or otherwise supported inmating contact with an external surface of the hollow cylinder (11005)to provide a thermally conductive coupling between an external surfaceof the hollow cylinder (11005) and the first thermal sensor (8030). Inthe example embodiment of FIG. 11, the first thermal sensor (8030) isthermally conductively coupled or otherwise supported in mating contactwith the external surface the hollow cylinder (11005) by one of aninwardly directed radial pressure force applied by the thermallyinsulating element (3080) disposed inside the catalyzing cavity (3035),as shown in FIG. 3 and described above, or by brazing, by a thermallyconductive bonding material, by one or more fasteners or clamps, or thelike.

Referring now to FIG. 12, a fourth exemplary, non-limiting conductiveelement embodiment comprises a spiral portion (12005) of a hollowcylinder. The spiral portion (12005) has an inner radius that is sizedto provide mating contact with the external surface (12010) of thecatalyzing body (3030), and an outer radius sized to provide a desiredthickness of the spiral portion of (12005). The spiral portion has alongitudinal axis (12015) that is oriented substantially coaxial withthe longitudinal axis (12020) of the catalyzing body (3030).

The spiral portion (12005) is formed with an annular wall thickness ofabout 1.6 mm and a longitudinal of length 12.7 to 25.4 mm, that is aboutone half (½) to the full longitudinal length of the catalyzing body(3030). The spiral portion (12005) may be longitudinally positioned tocontact the external surface (11010) of the catalyzing body (3030) atany longitudinal position between the interface end (3032) and theoutput end (3034). Other spiral portions (12005) having differentlongitudinal length and thickness dimensions are usable withoutdeviating from the present disclosure.

The first thermal sensor (8030) is attached to or otherwise supported inmating contact with an external surface of the spiral portion (12005) toprovide a thermally conductive coupling between an external surface ofthe spiral portion and the first thermal sensor (8030). In the exampleembodiment of FIG. 12, the first thermal sensor (8030) is thermallyconductively coupled or otherwise supported in mating contact with theexternal surface the spiral portion (12005) by one of an inwardlydirected radial pressure force applied by the thermally insulatingelement (3080), disposed inside the catalyzing cavity (3035), as shownin FIG. 3 and described above, or by brazing, thermally conductivebonding material, by one or more fasteners or clamps, or the like.

Referring now to FIGS. 13A and 13B, a cylindrical catalyzing body(13030) includes a plurality of catalyst fuel passages (3085) eachproviding an individual conduit that extends longitudinally through thecylindrical catalyzing body (13030). A central cavity (13007) is formedby a through hole, or a blind hole, that extends completely through orpartly through the cylindrical catalyzing body (13030) along alongitudinal axis (13020) thereof. As shown in the section view of FIG.13B, a fifth exemplary, non-limiting conductive element embodimentcomprises a solid cylinder (13005) disposed inside the central cavity(13007). A solid cylinder (13005) is supported inside the central cavity(13007) in mating contact with the inside diameter thereof. The solidcylinder (13005) has a longitudinal axis that extends substantiallycoaxial with the longitudinal axis (13020) of the catalyzing body(13030).

The solid cylinder (13005) is formed with an outside diameter sizedequal to, slightly greater than, or slightly less than the insidediameter of the central cavity (13007). A non-limiting exemplarydiameter of the solid cylinder (13005) is 1.5 to 6.4 mm in diameter witha longitudinal length of 6.3 to 12.7 mm, which is about one quarter (¼)to one half (½) of the longitudinal length of the catalyzing body(13030). The solid cylinder (13005) may be longitudinally positioned tocontact the central cavity (13007) at any longitudinal position betweenthe input or interface end (3032) and the output end (3034). Other solidcylinder (13005) embodiments having different longitudinal length andoutside cylinder diameter dimensions are usable without deviating fromthe present disclosure.

The first thermal sensor (8030) is attached to or otherwise supported bythe solid cylinder (13005) to provide a thermally conductive couplingbetween at least one surface of the solid cylinder (13005) and the firstthermal sensor (8030). In the example embodiment of FIG. 13B, the solidcylinder (13005) includes a through hole or a blind hole (13025) thatextends along or parallel with the longitudinal axis (13020) of thesolid cylinder (13005). The first thermal sensor (8030) is installedinto the through or blind hole (13025) and held in place. Alternately,the first thermal sensor (8030) is thermally conductively coupled to anyexternal or internal surface of the solid cylinder (13005) by brazing,by a thermally conductive bonding material, by one or more mechanicalfasteners or clamps, or the like.

Referring to FIG. 14 in a sixth exemplary, non-limiting embodimentcomprises a cylindrical catalyzing body (14030) formed as an open cellsolid foam structure comprising a solid, non-porous, ceramic foammaterial formed with a plurality of interconnecting open cellsdistributed through the solid ceramic foam structure. The open cellsextend between the input or interface end (3032) and the output end(3034); however, some open cells can extend from the input or interfaceend (3032) to sidewalls of the cylindrical catalyzing body (14030). Eachof the plurality of open cells (14031) includes inside surfaces thereofthat are coated with a catalyst layer (3090). The open cell solid foamstructure is formed as or is shaped as the cylindrical catalyzing body(14030) having a circumferential diameter of 25.4 mm and a longitudinallength of 25.4 mm. When installed into the cylindrical catalyzing cavity(3035), an input end (14032) of the cylindrical catalyzing body (14030)is inserted to contact the reactor shield base wall (3015) at theinterface (3032), and fuel air mixture (2025, 3025) exiting from thereactor shield base wall (3015) enters the input end of the solid foamstructure through the open cells (14031) thereof and passes through theopen cells to the output end (14034) or through open cell openings thatpass through the circumferential external surface (14010). While passingthrough the open cells, the fuel air mixture (2025, 3025) contacts thecatalyst layer (3090) to initiate the CPOX reaction. After exiting fromthe open cells, the reformed fuel or syngas (2027) passes from thecatalyzing cavity to the fuel inlet manifold (3055).

A prismatic rod (9005) is usable as a thermally conductive element. Asdescribed above the prismatic rod (9005) has a diameter of 3.2 mm thatis about one eighth (⅛) the diameter of the cylindrical catalyzing body(14030), and a longitudinal length of, 6.3 to 12.7 mm, that is about onequarter (¼) to one half (½) of the longitudinal length of thecylindrical catalyzing body (14030). The prismatic rod (9005) may belongitudinally positioned to contact the circumferential externalsurface (14010) at any longitudinal position between the interface end(13032) and the output end (13034). Similarly, any of the abovedescribed thermally conductive elements (10005, 11005, 12005, 13005) isusable in combination with the open cell solid foam structure of thecatalyzing body (14030).

The first thermal sensor (8030) is attached to or otherwise supported bythe prismatic rod (9005) to provide a thermally conductive couplingbetween at least one surface of the prismatic rod (9005) and the firstthermal sensor (8030). In the example embodiment of FIG. 14, theprismatic rod (9005) includes a through hole or a blind hole (9025)extending along the longitudinal axis (9015) thereof and the firstthermal sensor (8030) is installed into the through or blind hole(9025). Alternately, the first thermal sensor (8030) is thermallyconductively coupled to any external or inside surface of the prismaticrod (9005) by brazing, by a thermally conductive bonding material, byone or more fasteners of clamps, or the like.

The prismatic rod (9005) is attached to or otherwise supported in matingcontact with the circumferential external surface (14010) of thecylindrical catalyzing body (14030) by one of a radially applied inwardpressure force applied by the thermally insulating element (3080)disposed inside the catalyzing cavity (3035), as shown in FIG. 3, anddescribed above, or by brazing, by a thermally conductive bondingmaterial, by one or more fasteners or clamps, or the like.

8.12.9 Second Thermal Sensor:

Referring now to FIG. 8, a second thermal sensor (8040) is thermallyconductively coupled to an outside surface of one of the hot zoneenclosure walls (115), e.g. to an outside surface of the longitudinalcylindrical sidewall (2015), shown in FIG. 2. Alternately, the secondthermal sensor (8040) can be positioned on the inside or on an outsidesurface of any one of the hot zone enclosure walls that form the firstthermally conductive path. The second thermal sensor (8040) generates asecond temperature signal that is sampled by the electronic controllerat a sampling frequency that generates a continuous stream of secondtemperature signal values each corresponding with an instantaneoustemperature of a surface of one of the hot zone enclosure walls (115).However, since the hot zone enclosure walls (115) are thermallyconductively coupled with the disk shaped support walls (2082, 2084)that support opposing ends of each tubular fuel cell (2080), of the SOFCstack, variations in the temperature represented by changes in thesecond temperature signal correspond with or are proportional tovariations of the SOFC reaction temperature, e.g. when the O:C ratio ofthe incoming fuel is varied. Alternately, in other nonlimitingembodiments, the second thermal sensor (8040) is thermally conductivelycoupled to any surface of the intermediate enclosure (2510) that formsthe second thermally conductive path or to any one of the outerenclosure walls (2514, 2516, 2518) that form the third thermallyconductive path without deviating from the present disclosure, as longas variations in the temperature represented by changes in the secondtemperature signal correspond with or are proportional to variations ofthe SOFC reaction temperature, e.g. when the O:C ratio of the incomingfuel is varied.

8.12.10 Third Thermal Sensor:

Referring now to FIG. 3, a third thermal sensor (3135) is thermallyconductively coupled to a surface of the heat dissipating flange 3100,shown in FIG. 3. Alternately, the third thermal sensor (3135) can bepositioned on any surface of the fuel reactor body (3040) that extendsoutside the outer enclosure walls (2514, 2516, 2518) that form the thirdthermally conductive path. The third thermal sensor (3135) generates athird temperature signal that is sampled by the electronic controller ata sampling frequency that generates a continuous stream of thirdtemperature signal values each corresponding to an instantaneoustemperature corresponding a surface of the third thermally conductivepath associated with surfaces of the fuel reactor body (3040). However,since the third thermally conductive path also extends to elements thatdo not extend outside the outer enclosure walls, such as the annularperimeter wall (3010) and the reactor shield base wall (3015), changesin the third temperature signal ideally correspond with or areproportional to changes in temperature of the fuel reactor body, e.g.when the temperatures inside the fuel chamber approach the fuel autoignition temperature which range from 295 to 580° C., depending on thehydrocarbon fuel type.

8.12.11 Alternate Operating mode:

8.12.11.1 CPOX Reaction Temperature

Referring now to FIG. 8, in a non-limiting exemplary operating mode, afirst temperature signal (8031) is received, by the electroniccontroller (190), from the first thermal sensor (8030). The firsttemperature signal (8030) may comprise an analog or digital signalcorresponding with a voltage or current amplitude, a normalized voltageor current amplitude, or the like, wherein each different voltage orcurrent amplitude value of the first temperature signal (8031)corresponds with an actual instantaneous temperature or a relativeinstantaneous temperature being sensed by the first thermal sensor(8030). The electronic controller (190) stores a plurality of firsttemperature set point values. The plurality of first temperature setpoint values may comprise a different first temperature set point valuefor each hydrocarbon fuel type that will be used by the SOFC system,e.g. a first temperature set point value for propane (C₃H₈) and adifferent first temperature set point for natural gas or methane (CH₄),or the like. The plurality of first temperature set point values maycomprise a different first temperature set point value for eachoperating mode of the SOFC system, e.g. a first temperature set pointvalue associated with a start-up mode when the fuel is propane, and adifferent first temperature set point value associated with a steadystate operating mode when the fuel is propane, or the like. Theplurality of first temperature set point values may also comprise afirst temperature set point value associated with a maximum safeoperating temperature, e.g. when the fuel is methane, or the like.Additionally, each first temperature set point value may comprise arange of values e.g. defined by a maximum and a minimum firsttemperature set point value, defined by a median value with a plus orminus range, or the like.

Based on a calibration process, described below, each first temperatureset point value or range of first set point values corresponds with adesired syngas composition, e.g. when the syngas composition is free of,or substantially free of, unreacted hydrocarbon fuel and or hydrogen andcarbon based byproducts of the CPOX reaction. As an example, if thehydrocarbon fuel being used is methane, a desired first temperaturesetpoint value produces a syngas composition that is substantially freeof methane (CH₄) and other byproducts of the CPOX reaction, e.g.C₂H_(x), tar (C₁₀H₈), and other long chain hydrocarbon molecules,especially ones that can participate in coke formation, sulfides, e.g.carbon disulfide (CS₂), hydrogen sulfide (H₂S), sulfur dioxide (SO₂), orthe like, that can compete for oxygen sites at the solid oxide anodeelectrode layers (150) in the SOFC stack and or damage the solid oxideanode electrode layers (150). In another example, if the hydrocarbonfuel being used is propane, (C₃H₈), a desired first temperature setpointvalue produces a syngas composition that is substantially free ofpropane, methane, and the other byproducts of the CPOX reaction listedabove.

FIG. 15A depicts a graphical representation (1500) of calibration datathat is listed in the Table (1505) of FIG. 15B. The data includes O:C orOxygen to Carbon ratio of the incoming hydrocarbon fuel air mixture(2025, 3025), T_CPOX, or the first temperature in degrees Centigrade, %CH₄ and % C₂H_(x) based on weight percentage. Referring to FIG. 15A, theO:C ratio is shown along horizontal axis over a range of 1.2 to 1.5 andthe O:C ratio is plotted vs T_CPOX(C) or first temperature, shown on aleft vertical axis of FIG. 15A over a range of 608 to 630 degreesCentigrade. The data further includes weight percentage of undesirablehydrocarbon components such as methane (CH₄) and (C₂H_(x)), shown or aright vertical axis of FIG. 15A over a range of 0.0 to 0.3 percent. Thusthe right axis provides a measure of various undesirable byproducts ofthe CPOX reaction, e.g. C₂H_(x), tar (C₁₀H₈), and other long chainhydrocarbon molecules, especially ones that can participate in cokeformation, sulfides, e.g. carbon disulfide (CS₂), hydrogen sulfide(H₂S), sulfur dioxide (SO₂), or the like, that can compete for oxygensites at the solid oxide anode electrode layers (150) in the SOFC stackand or damage the solid oxide anode electrode layers (150).

As best viewed in FIG. 15A, a plot (1510) of O:C ratio vs T_CPOX (° C.)is linear. The plot (1510) shows that a temperature T_CPOX (° C.), whichcorresponds with the instantaneous temperature sensed by the firstthermal sensor (8030), increases linearly with increasing O:C ratio. Inother words, the temperature T_CPOX (° C.), increases as air is added tothe hydrocarbon fuel air mixture (2025, 3025).

Also, in FIG. 15A, a plot (1515) of O:C ratio vs % CH₄ is non-linear.The plot (1515) shows that a percentage of methane that remains in thesyngas composition decreases non-linearly with increased O:C ratio.Thus, the percentage of unreacted methane decreases as the O:C ratioincreases and as T_CPOX increases in response to the increased O:C ratiountil the O:C ratio reaches 1.4 or above, when the percentage ofunreacted methane is substantially zero. As further demonstrated in FIG.15A, the O:C ratio of 1.4 corresponds with the T_CPOX temperature of628° C. Also, in FIG. 15A, a plot (1520) of O:C ratio vs % C₂H_(x) isnot clearly linear of non-linear. The plot (1520) shows that apercentage of % C₂H_(x) that remains in the syngas composition isundetectable.

Thus, FIG. 15A clearly demonstrates that by detecting the temperatureT_CPOX, corresponding with the first temperature signal (8031), the O:Cratio and the syngas composition can be characterized, based on theT_CPOX value alone, at least to the extent that a T_CPOX temperature setpoint value or range of set point values (1530), can be selected tocorrespond with eliminating undesirable hydrocarbon components such asmethane (CH₄) (C₂H_(x)), and other long chain hydrocarbon molecules fromthe syngas being generated. More specifically, a CPOX reaction beingcarried while the T_CPOX temperature is maintained at a set point valuewithin a range of set point values (1530) shown in FIG. 15A will be freeof undesirable hydrocarbon components. Moreover, the T_CPOX temperaturecan be controlled simply by varying the oxidant flow rate alone. Thus,based on the plots shown in FIG. 15A, and the data listed in FIG. 15B, afirst temperature set point range (1530), corresponds with a set pointtemperature T_CPOX (C) of between about 618 and 623 degrees C. whichcorresponds with an O:C ratio range of between about 1.38 and 1.42.During steady state operation, the electronic controller (190) samplesthe first temperature signal (8031) at the sampling frequency togenerate a continuous stream of first temperature signal values (8031),each corresponding to an instantaneous temperature of the thermallyconductive element supported in mating contact with the catalyzing body,shown in any one of FIGS. 9-14 above. The electronic controller compareseach first temperature signal value (8031) with an appropriate set pointtemperature value, or appropriate range of set point values. The setpoint values are stored by the electronic controller and different setpoint values, or set point value ranges, may correspond with differenthydrocarbon fuel types, with different SOFC system configurations, withdifferent thermally conductive element types, and other operatingparameters, e.g. operating mode, oxidant type, fuel air mixturetemperature, DC power output of the SOFC system, or the like. When asampled first temperature signal value (8031) is equal to theappropriate first temperature set point value or within the range ofappropriate first temperature set point values, no action is taken bythe electronic controller. When the sampled first temperature signalvalue is not equal to the appropriate first temperature set point valueor not within the range of appropriate first temperature set pointvalues, the electronic controller makes a logical conclusion to eitherincrease or decrease the oxidant flow rate being delivered into themixing chamber (8015) and then transmits one or more command and controlsignals to the oxidant flow modulator (8025) wherein the command andcontrol signals correspond with either increasing or decreasing theoxidant flow rate as demanded by the logical conclusion.

In one non-limiting exemplary operating mode, when the sampled firsttemperature signal value (8031) is less than a minimum acceptable firstsignal value, the electronic controller (190) commands the oxidant flowmodulator (8025) to increase the mass or volume flow rate of oxidantentering the mixing chamber (8015) to thereby increase the O:C ratio,which results in an increase of the CPOX reaction temperature and acorresponding increase in the temperature T_CPOX (° C.) andcorresponding first temperature signal value (8031). Alternately, whenthe sampled first temperature signal is greater than a maximumacceptable first temperature signal value (8031), the electroniccontroller (190) commands the oxidant flow modulator (8025) to decreasea mass or volume flow rate of oxidant entering the mixing chamber (8015)which results in a decrease of the CPOX reaction temperature. In eachcase, the increase or decrease of the CPOX reaction temperature resultsin a corresponding proportional increase or decrease in the temperatureof the thermally conductive element thermally conductively coupledbetween the catalyzing body (9005, 10005, 11005, 12005, 13005) and firstthermal sensor (8030). In a non-limiting exemplary embodiment, the firstsignal sampling rate ranges between about 5 Hz and 100 KHz. In anon-limiting exemplary embodiment, a minimum incremental change in thevolume flow rate of the oxidant ranges between 0.1 to 2.0 Standard CubicCentimeters per minute (SCCM).

8.12.11.2 SOFC Reaction Temperature

In an exemplary operating mode, a second temperature signal (8041) isreceived, by the electronic controller (190), from the second thermalsensor (8040). The second temperature signal (8041) may comprise ananalog or digital signal corresponding with a voltage or currentamplitude, a normalized voltage or current amplitude, or the like,wherein each different voltage or current amplitude value of the secondtemperature signal (8041) corresponds with a different temperature beingsensed by the second thermal sensor (8040). The electronic controller(190) stores one of more second temperature set point values. Eachsecond temperature set point value corresponds with a second temperaturesignal value or range of values that corresponds with an SOFC reactiontemperature that produces a desired result.

The desired result may comprise any one of a threshold for DC power orcurrent generation by the SOFC fuel cell stack or a DC power or currentoutput value corresponding with median, maximum, or other DC power orcurrent amplitude output. Other desired result criteria are acomposition of exhaust gas exiting from the system exhaust port (2165),or the exhaust gas exiting from the SOFC tubes into the combustionchamber (2135), e.g. when the exhaust gas composition is substantiallyfree of unreacted anode gas components, H₂ and CO, and/or free ofbyproducts that may indicate an incomplete conversion of the anode gasto electrical power. Still other desired result criteria are variousmeasurable characteristics of an efficiency of the fuel cell, e.g.electrical energy output per unit volume of hydrocarbon fuel input, orthe like.

As described above with respect to the first set point temperaturevalues, each fuel type and each operating mode of the SOFC system, mayhave a different second temperature set point value that correspondswith only one hydrocarbon fuel type or only one operating mode, so theelectronic controller (190) preferably stores a different secondtemperature set point value for each of a plurality of differenthydrocarbon fuel types, for each operating mode, or the like.Accordingly, the electronic controller (190) may also sense thehydrocarbon fuel type being used by the SOFC system or a user may inputhydrocarbon fuel type and other parameters of the SOFC system. Eitherway, the electronic controller selects an appropriate second temperatureset point value that corresponds with the fuel type, operating mode, orthe like.

The second temperature set point value stored by the electroniccontroller (190) may include one second temperature signal value or arange of second temperature signal values that correspond with thesecond temperature set point. A correlation between the desired DC poweroutput and the second temperature set point value or range of secondtemperature signal values is determined by a system calibrationdescribed below. In addition to storing the plurality of second setpoint values or ranges, corresponding with different hydrocarbon fueltypes, the electronic controller may further store other temperaturesignal values that correspond with other desirable operating conditionssuch as, a safe maximum operating temperature, a minimum or thresholdtemperature for DC power generation, or the like.

The electronic controller (190) periodically samples the secondtemperature signal (8041) received thereby and compares the sampledsecond temperature signal value with an appropriate second temperatureset point or second temperature set point range of values. If thesampled second temperature signal is equal to the second temperature setpoint or within the second set point range, no action is taken by theelectronic controller. If the sampled second temperature signal is notequal to the second temperature set point value or is not within thesecond set point range of values, the electronic controller makes alogical conclusion to either increase or decrease the hydrocarbon fuelflow rate being delivered into the mixing chamber (8015) and thentransmits one or more control and command signals to the hydrocarbonfuel flow modulator (8035), wherein the control signals correspond witheither increasing or decreasing the hydrocarbon fuel flow rate to themixing chamber (8015).

In one non-limiting exemplary operating mode, when the secondtemperature signal value is less than a minimum acceptable secondtemperature signal value, the electronic controller (190) commands thehydrocarbon flow modulator (8035) to increase the mass or volume flowrate of hydrocarbon fuel entering the mixing chamber (8015).Alternately, when the sampled second temperature signal is greater thana maximum acceptable second temperature signal value, the electroniccontroller (190) commands the hydrocarbon fuel flow modulator (8035) todecrease a mass or volume flow rate of hydrocarbon fuel entering themixing chamber (8015). In the first instance, the increase in the flowrate of hydrocarbon fuel entering the mixing chamber (8015) increasesthe volume of hydrocarbon fuel being converted to syngas whichultimately increases the temperature of the syngas and of the tubularSOFC rods and this increase in temperature ultimately increases thetemperature of the outer enclosure walls being sensed by the secondthermal sensor (8040). In the second instance, the decrease in the flowrate of hydrocarbon fuel entering the mixing chamber (8015) decreasesthe volume of hydrocarbon fuel being converted to syngas whichultimately decreases the temperature of the syngas and of the tubularSOFC rods and this decrease in temperature ultimately decreases thetemperature of the outer enclosure walls being sensed by the secondthermal sensor (8040).

In this manner, the electronic controller (190) periodically samples thesecond signal (8041) generated by the second thermal sensor (8040) at asecond signal sampling rate; and makes appropriate adjustments toincrease or decrease the temperature being sensed by the second thermalsensor (8040) by increasing or decreasing the mass or volume flow rateof hydrocarbon fuel entering the mixing chamber (8015). The secondsignal sampling rate ranges between about 5 Hz and 100 KHz. The minimumincremental change in the volume flow rate of the hydrocarbon fuelranges between 0.1 and 2.0 Standard Cubic Centimeters per minute (SCCM).

As will be recognized by those skilled in the art, when the oxidant flowrate to the mixing chamber (8015) is varied without also varying thehydrocarbon fuel flow rate, the O:C ratio is changed. Similarly, whenthe hydrocarbon fuel flow rate to the mixing chamber (8015) is variedwithout also varying the oxidant flow rate, the O:C ratio is alsochanged. As demonstrated by the plots of FIG. 15A, O:C ratio changes,whether resulting from only changing the oxidant flow rate, or onlychanging the hydrocarbon fuel flow rate, result in changes in thetemperature being sensed by first thermal sensor (8030). Similarly, O:Cratio changes, whether resulting from only changing the oxidant flowrate, or only changing the hydrocarbon fuel flow rate, result in changesin composition of the syngas, with an increase in methane contentoccurring as the O:C ratio drops below about 1.35.

According, to one non-limited exemplary operating method of the presentdisclosure, a first control loop is operated by the electroniccontroller (190). In the first control loop, the first thermal sensor(8030) is sampled at a first sampling rate, e.g. 50 Hz, with each sampleproviding a first temperature signal value corresponding with the firstthermal sensor (8030). Additionally, the oxidant flow modulator (8025)is controlled to adjust the oxidant flow rate to either increase ordecrease the oxidant flow rate as required to maintain the firsttemperature signal value at the set point value or within the range ofset point values corresponding with the first temperature signal storedby the electronic controller. While the oxidant flow modulator (8025)can be adjusted at the same rate as the first sampling rate of 50 Hz,the first sampling rate of the first temperature signal value and theadjustment rate of the oxidant flow modulator (8025) can differ.Preferably the first control loop is operated independently of a secondcontrol loop described below.

The non-limited exemplary operating method further includes operating asecond control loop by the electronic controller (190). In the secondcontrol loop, the second thermal sensor (8040) is sampled at a secondsampling rate, e.g. 50 Hz, with each sample providing a secondtemperature signal value corresponding with the second thermal sensor(8040). Additionally, the hydrocarbon fuel flow modulator (8035) iscontrolled to adjust the hydrocarbon fuel flow rate to either increaseor decrease the hydrocarbon fuel flow rate as required to maintain thesecond temperature signal value at the set point value or within therange of set point values corresponding with the second temperaturesignal stored by the electronic controller. While the hydrocarbon fuelflow modulator (8035) can be adjusted at the same rate as the secondsampling rate of 50 Hz, the sampling rate of the second temperaturesignal value and the adjustment rate of the hydrocarbon fuel flowmodulator (8035) can differ. Preferably the second control loop isoperated independently of a first control loop described above.

The non-limited exemplary operating method further includes operating athird control loop by the electronic controller (190). In the thirdcontrol loop, each second temperature signal value corresponding withthe second thermal sensor (8040) is compared with a control failsafetemperature corresponding with the location of the second thermal sensorthat is stored by the electronic controller (190). The control failsafetemperature corresponding with the location of the second thermal sensoris a maximum safe operating temperature for the location of the secondthermal sensor (8040), which for the present example embodiment is asurface of the hot zone enclosure wall, or any other surface of thefirst thermally conductive pathway. When the control failsafetemperature corresponding with the location of the second thermal sensoris detected by the electronic controller, the electronic controller isconfigured to close the hydrocarbon fuel flow modulator (8035) to stopfurther fuel flow into the mixing chamber (8015). While the hydrocarbonfuel flow modulator is closed, the electronic controller is configuredto fully open the oxidant and cathode gas flow modulators (8025, 8050)to pump oxidant through the SOFC system for cooling.

The non-limited exemplary operating method further includes operating afourth control loop by the electronic controller (190). In the fourthcontrol loop, the SOFC system is purposely operated with a high O:Cratio e.g. corresponding with an elevated first thermal sensor valueT_CPOX, as shown in the plot (1510) in FIG. 15A. The selected elevatedsensor value T_CPOX, for the fourth control loop, is greater than thesetpoint sensor value T_CPOX or range of sensor values T_CPOX (1530)used during normal operation. The fourth control loop may be used duringa startup mode, e.g. to more rapidly heat the SOFC system to an SOFCreaction temperature, e.g. sensed as by the second thermal sensor(8040). The fourth control loop may also be used to purposely over heatthe SOFC system as a means for cleaning the catalyst layer (3090) andsolid oxide anode electrode layers (150), e.g. to burn off tar deposits,or the like.

The fourth control loop is initiated to operate the SOFC system with anO:C ratio corresponding with the elevated first thermal sensor signalT_CPOX. In the example calibration chart of FIG. 15A, the elevated firstthermal sensor signal T_CPOX at least corresponds with an O:C ratiogreater than about 1.4. In one non-limiting embodiment, the fourthcontrol loop in configured to run the SOFC system with an O:C ratio of1.5 or greater, for a predetermined time period or until the elevatedfirst thermal sensor signal T_CPOX reaches an upper setpoint valuecorresponding with a maximum first thermal sensor signal T_CPOX.

The fourth control loop includes a stored value or range of valuesassociated with an elevated first thermal sensor signal,T_CPOX-elevated. The T_CPOX-elevated values provide a correspondingelevated O:C ratio that is greater than the O:C ratio corresponding withthe setpoint temperature or set point temperature range (1530) used fornormal operation. Preferably, the elevated O:C ratio is in a range of2.0 to 2.2. Alternately the elevated temperature T_CPOX-elevated is arange of temperature values corresponding with the first temperaturesignal (8031) that provides an O:C ratio between about 2.0 and 2.2.

One non-limiting exemplary implementation of the fourth control loop isto change the set point value or range of values (1530) correspondingwith first thermal sensor signal used for normal operation to theT_CPOX-elevated set point value or range of values corresponding withthe desired elevated O:C ratio and then allow the fourth control loop tomodulate oxidant flow rate as required to increase the first temperaturesignal values to comply with the T_CPOX-elevated set point value orrange of values, without changing the hydrocarbon fuel flow rate. Afterthe desired duration at the elevated temperature or O:C ratio, thefourth control loop ends its operation and changes the elevatedtemperature T_CPOX-elevated set point value or range of values back tothe set point value or range of values (1530) corresponding with firstthermal sensor signal used for normal operation and returns control backto the first and second control loops. Other parameters usable to endoperation of the fourth control loop include, monitoring the secondtemperature signal (8041) and or monitoring the DC power or currentamplitude generated by the SOFC stack as a means for determining whenthe SOFC stack has reached an acceptable operating temperature, or thelike.

8.11.13 Calibration Procedure

According to the present disclosure an optimization process is carriedout to maximize the weight percentage of the anode gas components H₂ andCO of the syngas, while also minimizing the weight percentage ofunreacted hydrocarbons e.g. CH₄, C₂H_(x) and other longer hydrocarbonmolecule chains including ethane (C₂H₆) propane (C₃H₈), butane (C₄H₁₀),or the like. In some calibration procedures, the optimization processalso includes characterizing the weight percentage of other componentsof the syngas (2027) such as oxygen gas, water, nitrogen gas, carbonmonoxide, carbon dioxide, tar (C₁₀H₈), and sulfides, including carbondisulfide (CS₂), hydrogen sulfide (H₂S), sulfur dioxide (SO₂), or thelike. More generally, the optimization process is carried out toidentify a primary set point value or range of set point valuescorresponding with the first temperature signal (8031). The primary setpoint value, or range of set point values correspond with valuesgenerated by the first thermal sensor (8030) that correspond with arepeatable desired result related to a characteristic of the CPOXreaction. As noted above the desired result is a desired syngascomposition; however, a different and simpler desired result is a weightpercentage of methane of less than 0.01%, or the like.

The optimization process is performed to qualify a system design basedon a specific hydrocarbon fuel type. The system design includes theconfiguration and location of the thermally conductive element, (9005,10005, 11005, 12005, 13005), the configuration and location of the firstthermal sensor (8031) with respect to the thermally conductive element,the configuration and physical dimensions of the catalyst body (3030),the configuration and location of the second thermal sensor (8040) andthe repeatable desired result selected to characterize the CPOXreaction.

In a first calibration step, the SOFC system is installed into acalibration tool or fixture that includes elements provided to measurevarious operating parameters of the SOFC system, such as DC output powerand or current generated by the SOFC system oxidant and hydrocarbon fuelflow rates, e.g. in the conduits (8017) and (8022), cathode gas flowrate, e.g. in the conduit (8055), syngas gas composition, e.g. in theinput manifold (3055), and exhaust gas composition at the exit of theSOFC stack, e.g. in the combustion chamber (2135).

The calibration tool or fixture includes at least one gas chromatographprobe positioned to sample syngas exiting from the catalyzing body(3030) and a gas chromatograph configured to make the desired syngascomposition analysis. Optionally, a second gas chromatograph probe ispositioned to sample exhaust gas exiting from the SOFC stack, e.g.positioned inside the combustion chamber (2135) and a second gaschromatograph is configured to make the desired exhaust gas compositionanalysis. The calibration tool or fixture also provides a mass of volumeflow rate meter associated with each of the oxidant flow modulator(8025) and the hydrocarbon fuel modulator (8035) and optionally, thecathode flow modulator (8050) for measuring appropriate gas flow rates.The calibration tool or fixture includes a calibration controllerconfigured to operate the SOFC system, e.g. to sample thermal sensorsignals (8031) and (8040), to sample DC power output values, e.g.current and/or power amplitude, to modulate oxidant, hydrocarbon fuel,and cathode air flow rates, to sample the flow rate meters, to store setpoint values, to analyze and store gas composition data, to determineand select set point values or ranges of values for each of the thermalsensors signals (8031) and (8040), or the like. The calibrationcontroller is configured to collect gas chromatograph sample data, flowmeter data and first and second thermal sensor data, and perform logicaloperations related to carrying out a calibration process by analyzingdata associated with achieving one or more repeatable desired resultsrelated to a characteristic of the CPOX reaction and/or related toachieving the repeatable desired result related to a characteristic ofthe SOFC reaction.

In a second calibration step the SOFC system is brought to a steadystate operating mode wherein an SOFC reaction has been initiated and theSOFC system is generating DC power. Thereafter operating parameters ofthe SOFC system are varied by the calibration controller as required toachieve the repeatable desired result related to a characteristic of theSOFC reaction. As noted above, the desired result related to acharacteristic of the SOFC reaction can be associated withcharacteristics of the DC power or current output. In one example, thesecond signal values output by the second thermal sensor (8040) aremonitored over a range of hydrocarbon fuel flow rates while the oxidantflow rate is held constant, to plot DC power output over a range of O:Cratios. In one non-limiting example embodiment, the calibration systemmay select a second temperature signal set point value, or range ofsecond temperature signal set point values corresponding with a DC poweroutput characteristic such as, a set point corresponding with initiationof the DC power output, a set point corresponding with maximumobtainable DC power output and a set point corresponding with a medianDC power output.

In another non-limiting example embodiment, the calibration system mayselect a second temperature signal set point value, or range of secondtemperature signal set point values corresponding to a composition ofthe exhaust gas exiting from the SOFC stack that demonstrates that theexhaust gas is substantially free of anode gas components. In stillanother non-limiting example embodiment, the calibration system mayselect a second temperature signal set point value, or range of secondtemperature signal set point values, or a ratio of hydrocarbon fuel flowrate input to DC current output, or the like. Irrespective of whichdesired output of the SOFC system is being evaluated to determine thesecond signal values output by the second thermal sensor (8040), thesecond signal values output by the second thermal sensor (8040) aremonitored over whatever range of hydrocarbon fuel flow rates is usedwhile the oxidant flow rate is held constant, to plot the desired outputof the SOFC system vs O:C ratios. Additionally, these plots may berepeated for one or more different oxidant flow rates in order to findan optimum O:C ratio and corresponding optimum second signal value orrange of values corresponding with the desired output of the SOFCsystem.

In a third calibration step, a weight percentage of each syngascomponent or selected syngas components is determined by analyzing asample of the syngas by a gas chromatograph over a plurality ofdifferent O:C ratios. The O:C ratios are varied by only modifying theoxidant flow rate, which is a process that is carried out by thecalibration controller. During the third calibration step, thehydrocarbon fuel flow rate is not changed. The calibration controlleralso samples the first temperature signal (8031) and the oxidant flowrate meter data over the plurality of different O:C ratios and storesthe first signal values and the oxidant flow rate values. Thecalibration controller is configured to analyze the syngas componentweight percentage for each O:C ratio and associate a first temperaturesignal value and oxidant flow rate value with each O:C ratio.Additionally, during the third calibration step, the calibrationcontroller is configured to monitor, and record data associated with thedesired output of the SOFC system. The data related with desired outputof the SOFC system at least includes: the second temperature signal(8041) at each O:C ratio and one or more of, the hydrocarbon fuel andcathode air flow rate, a DC output power characteristic of the SOFCstack, a composition of the exhaust gas exiting from the SOFC stack asdetermined from gas chromatograph data, or the like.

In a fourth calibration step, the weight percentage of each syngascomponent corresponding with each of the plurality of different O:Cratios generated by the third calibration step is analyzed to determinewhich O:C ratios constantly produce the desired syngas composition, e.g.with a weight percentage of methane of less than 0.01%, or the like. Thefourth calibration step further includes determining, by the calibrationcontroller, the first temperature signal value, or range of firsttemperature signal values degenerated by the first thermal sensor (8030)that are associated with providing the desired syngas composition. Asshown by plot (1510) in FIG. 15A, the first set point value or range ofvalues (1530) corresponds with the lowest temperature of firsttemperature signal value T_CPOX that meets the desired syngascomposition. However, other higher temperature values can be selectedwithout deviating from the present disclosure. Once the first set pointvalue or range of set point values (1530) is selected, using the fixedhydrocarbon fuel flow rate, corresponding with the second set pointvalue or range of values corresponding with the second thermal sensor(8040), the fourth calibration process can be rerun using other fixedhydrocarbon fuel flow rates in order to make refinements of the SOFCsystem operation by making small changes in each of the first and secondset point values.

When using the calibration fixture, the calibration procedure need onlybe performed once for a given SOFC system configuration using a givenhydrocarbon fuel type to determine the CPOX reaction temperature setpoint associated with the first thermal sensor (8030) and the SOFC stacktemperature set point associated with the second thermal sensor (8040).

The calibration fixture optionally also includes a plurality ofdifferent hydrocarbon fuel sources each corresponding with a differenthydrocarbon fuel type to calibrate the SOFC system for each of theplurality of different hydrocarbon fuel types. Thus, a fifth calibrationstep includes repeating calibration steps two though four for each ofthe plurality of different hydrocarbon fuel types which can result inselecting different CPOX reaction temperature set points and differentSOFC stack temperature set points for each different hydrocarbon fueltype.

It will also be recognized by those skilled in the art that, while theinvention has been described above in terms of preferred embodiments, itis not limited thereto. Various features and aspects of the abovedescribed invention may be used individually or jointly. Further,although the invention has been described in the context of itsimplementation in a particular environment, and for particularapplications (e.g. a solid oxide fuel system that includes a fuelreformer module carrying out an exothermic reaction to reformcombustible fuels housed therein), those skilled in the art willrecognize that its usefulness is not limited thereto and that thepresent invention can be beneficially utilized in any number ofenvironments and implementations where it is desirable to manage thermalenergy in high temperature corrosive environments where flammablematerials are processed. Accordingly, the claims set forth below shouldbe construed in view of the full breadth and spirit of the invention asdisclosed herein.

What is claimed is:
 1. A fuel reformer module for initiating catalyticpartial oxidation (CPOX) to reform a hydrocarbon fuel oxidant mixtureand deliver a syngas reformate therefrom comprising: a catalyzing body,having an input end and an output end comprising a solid non-porousceramic substrate formed to include a plurality of catalyst fuelpassages extending between the input end and one of the output end ofthe catalyzing body and a fuel passage output end that is not at theoutput end of the catalyzing body; a catalyst layer, comprising amaterial selected to initiate the CPOX reaction, formed onto an insidesurface of each of the plurality of catalyst fuel passages; a thermallyconductive element, comprising a material having a coefficient ofthermal conductivity of 50 W/m° K or greater, thermally conductivelycoupled with the catalyzing body over a contact surface area; and afirst thermal sensor, thermally conductively coupled with the thermallyconductive element, for generating a first temperature signalcorresponding with a temperature sensed by the first thermal sensor. 2.The fuel reformer of claim 1 wherein the input end and the output endare separated by a first longitudinal dimension that extends along alongitudinal axis of the catalyzing body and the contact surface areahas a second longitudinal dimension that extends along the longitudinalaxis, wherein the second longitudinal dimension is at least one quarterof the first longitudinal dimension.
 3. The fuel reformer of claim 2wherein the second longitudinal dimension is in a range of one quarterto one half of the first longitudinal dimension.
 4. The fuel reformer ofclaim 2 wherein the second longitudinal dimension is in a range of onequarter of to equal to the first longitudinal dimension.
 5. The fuelreformer of claim 1 wherein the catalyzing body is cylindrical with afirst longitudinal dimension that extends along a first longitudinalaxis of the catalyzing body between the input end and the output end andwith an outside diameter dimension that is centered by the longitudinalaxis.
 6. The fuel reformer of claim 5 wherein the first longitudinaldimension is 25 mm or larger and outside diameter dimension is 25 mm orlarger.
 7. The fuel reformer of claim 1 wherein the contact surface areais sized to promote a high enough rate of thermal conductivity betweenthe catalyzing body and the thermally conductive element for the firstthermal sensor to sense a change in an average temperature of thecontact surface area of 1 to 2 degrees centigrade in less than 30seconds.
 8. The fuel reformer of claim 1 wherein a material volume ofthe thermally conductive element is sized to promote a high enough rateof thermal conductivity between the catalyzing body and the thermallyconductive element for the first thermal sensor to sense a change in anaverage temperature of the contact surface area of 1 to 2 degreescentigrade in less than 30 seconds.
 9. The fuel reformer of claim 1wherein each of the contact surface area and a material volume of thethermally conductive element is sized to promote a high enough rate ofthermal conductivity between the catalyzing body and the thermallyconductive element for the first thermal sensor to sense a change in anaverage temperature of the contact surface area of 1 to 2 degreescentigrade in less than 30 seconds.
 10. The fuel reformer of claim 1wherein the input end and the output end are separated by a firstlongitudinal dimension that extends along a longitudinal axis of thecatalyzing body and wherein each of the plurality of catalyst fuelpassages extends, between the input end and the output end, alongdifferent fuel passage longitudinal axis that is parallel the firstlongitudinal axis.
 11. The fuel reformer of claim 5 wherein thenon-porous ceramic substrate comprises a solid, non-porous ceramic foammaterial, and the plurality of catalyst fuel passages comprises aplurality of interconnecting open cells extending between the input end,and one of, the output end of the catalyzing body, and the fuel passageoutput end that is not at the output end of the catalyzing body.
 12. Thefuel reformer of claim 5 wherein the thermally conductive elementcomprises a prismatic rod disposed in mating contact with the outsidediameter of the catalyzing body and wherein a longitudinal axis of theprismatic rod is oriented substantially parallel with the firstlongitudinal axis.
 13. The fuel reformer of claim 11 wherein thethermally conductive element comprises a prismatic rod disposed inmating contact with the outside diameter of the catalyzing body andwherein a longitudinal axis of the prismatic rod is orientedsubstantially parallel with the first longitudinal axis.
 14. The fuelreformer of claim 5 wherein the thermally conductive element comprises acylindrical segment disposed in mating contact with the outside diameterof the catalyzing body and wherein a longitudinal axis of thecylindrical segment is oriented substantially parallel with the firstlongitudinal axis and wherein the cylindrical segment includes a contactsurface area that is formed with a radius of curvature that is matchedwith a radius of curvature of an outside circumferential surface of thecylindrical catalyzing body.
 15. The fuel reformer of claim 5 whereinthe thermally conductive element comprises a hollow cylinder, having aninside diameter thereof, disposed in mating contact with the outsidediameter of the catalyzing body, wherein a longitudinal axis of thehollow cylinder is oriented substantially parallel with the firstlongitudinal axis, wherein the hollow cylinder is formed with an insidediameter sized to substantially match the outside diameter of thecatalyzing body, and the hollow cylinder is formed with an outsidediameter sized to provide a desired thickness of an annual wall formedby the hollow cylinder.
 16. The fuel reformer of claim 5 wherein thethermally conductive element comprises a spiral portion of a hollowcylinder, having an inside diameter thereof, disposed in mating contactwith the outside diameter of the catalyzing body, wherein a longitudinalaxis of the spiral portion of the hollow cylinder is orientedsubstantially parallel with the first longitudinal axis, wherein thespiral portion of the hollow cylinder is formed with an inside diametersized to substantially match the outside diameter of the catalyzingbody, and with an outside diameter, of the spiral portion of the hollowcylinder, sized to provide a desired thickness of a spiral annual wallformed by the spiral portion of the hollow cylinder.
 17. The fuelreformer of claim 5 wherein the catalyzing body is formed to include acentral cylindrical cavity that extends completely through or partlythrough the cylindrical catalyzing body, wherein the central cylindricalcavity is formed with an inside diameter, wherein the thermallyconductive element comprises a solid cylindrical element disposed insidethe central cylindrical cavity, wherein the central cylindrical cavityinside diameter is sized to substantially match an outside diameter ofthe solid cylindrical element and wherein the contact surface areaformed between the solid cylindrical element and the central cylindricalcavity and the material volume of the solid cylindrical element are eachsized to promote a high enough rate of thermal conductivity between thecatalyzing body and the thermally conductive element for the firstthermal sensor to sense a change in an average temperature of thecontact surface area of 1 to 2 degrees centigrade in less than 30seconds.
 18. An SOFC system comprising the fuel reformer module of claim1 and further comprising: a fuel oxidant control module configured togenerate the hydrocarbon fuel oxidant mixture by mixing hydrocarbon fuelreceived from a hydrocarbon fuel supply source with oxidant receivedfrom an oxidant supply source for delivery into the input end of thecatalyzing body, wherein the fuel oxidant control module includes ahydrocarbon fuel flow rate modulator disposed between the hydrocarbonfuel source and the input end and an oxidant flow rate modulatordisposed between the oxidant source and the input end; an electroniccontroller operating to transmit independent command and control signalsto each of the hydrocarbon fuel flow rate modulator and the oxidant flowrate modulator; a solid oxide fuel cell (SOFC) stack comprising aplurality individual SOFC fuel cells each comprising a solid oxide anodeelectrode layer, wherein the syngas reformate, output from the fuelreformer module, flows over the solid oxide anode electrode layers toinitiate and maintain an SOFC reaction; a hot zone enclosure comprisinga plurality of hot zone enclosure walls joined together to enclose a hotzone cavity surrounding the SOFC stack wherein the hot zone enclosurewalls are formed from materials having a coefficient of thermalconductivity of 100 W/m° K or greater and joined together to form afirst continuous thermally conductive pathway; a second thermal sensor,thermally conductively coupled with a surface of the first thermallyconductive pathway, for generating a second temperature signalcorresponding with a temperature of the surface of the first thermallyconductive pathway; a range of first set point temperature values,stored by the electronic controller, wherein the range of first setpoint values corresponds with a calibrated operating temperature rangecorresponding with a range of first temperature signal values that isknown to produce the syngas reformate with a desired syngas composition;a range of second set point temperature values, stored by the electroniccontroller, wherein the range of second set point values correspondswith a calibrated operating temperature range of second temperaturesignal values that is known to produce a desired performancecharacteristic of the SOFC stack; wherein the electronic controlleroperates a first control loop based on sampling the first thermal sensorsignal values, wherein the first control loop commands the oxidant flowrate modulator to increase or decrease the oxidant flow rate to maintainthe sampled first temperature signal values within the range of firstset point values; and, wherein the electronic controller operates asecond control loop based on sampling second thermal sensor signalvalues, wherein the second control loop commands the hydrocarbon fuelflow rate modulator to increase or decrease the hydrocarbon fuel flowrate to maintain the sampled second temperature signal values within therange of second set point values.
 19. A method comprising: delivering,by a fuel oxidant control module, into the fuel reformer module of claim1, the hydrocarbon fuel oxidant mixture, wherein the fuel oxidantcontrol modulator includes, a hydrocarbon fuel flow rate modulatordisposed between a hydrocarbon fuel supply source and the input end ofthe catalyst body, and an oxidant flow rate modulator disposed betweenan oxidant supply source and the input end of the catalyst body;delivering first command and control signals, from an electroniccontroller, to the oxidant flow rate modulator, to modulate an oxidantflow rate; delivering second command and control signals, from anelectronic controller, to the hydrocarbon fuel flow rate modulator, tomodulate a hydrocarbon fuel flow rate; delivering, the syngas reformateoutput, from the catalyst body, to a solid oxide fuel cell (SOFC) stack,wherein the SOFC stack comprises a plurality individual SOFC fuel cellseach including a solid oxide anode electrode layer in fluidcommunication with the syngas reformate output from the catalyst body,wherein the syngas reacts with the solid oxide anode electrode layers toinitiate an SOFC reaction at an SOFC reaction temperature; sampling, bythe electronic controller, first temperature control signal valuesgenerated by the first temperature sensor; sampling, by the electroniccontroller, second temperature control signal values generated by asecond temperature sensor, wherein the second thermal sensor ispositioned to sense a temperature of a surface that changes temperaturein proportion with temperature changes of the SOFC reaction temperature;storing, by the electronic controller, a range of first set pointtemperature values wherein the range of first set point valuescorresponds with a calibrated operating temperature range correspondingwith a range of first temperature signal values that is known to producethe syngas reformate with a desired syngas composition; storing, by theelectronic controller, a range of second set point temperature valueswherein the range of second set point values corresponds with acalibrated operating temperature range corresponding with a range ofsecond temperature signal values that is known to produce a desiredperformance characteristic of the SOFC stack; operating, by theelectronic controller, a first control loop based on sampling firsttemperature sensor signal values, wherein the first control loopcommands the oxidant flow rate modulator to increase or decrease theoxidant flow rate to maintain the sampled first temperature signalvalues within the range of first set point values; and, operating, bythe electronic controller, a second control loop based on samplingsecond thermal sensor signal values, wherein the second control loopcommands the hydrocarbon fuel flow rate modulator to increase ordecrease the hydrocarbon fuel flow rate to maintain the sampled secondtemperature signal values within the range of second set point values.20. The method of claim 19 wherein the step of storing, by theelectronic controller, a range of first set point temperature valuescorresponding with a desired composition of the syngas reformate beingoutput from the fuel reformer module further comprises, storing by theelectronic controller, a plurality of ranges of first set pointtemperature values with each range of first set point valuescorresponding with a plurality of different hydrocarbon fuel types,wherein the plurality of different hydrocarbon fuel types at leastincludes anyone of methane, (CH₄), ethane (C₂H₆), propane (C₃H₈), andbutane (C₄H₁₀).